Patent Application
20220219136
The present applicantion claims the priority of a patent application No. 201910471632.9, titled “a method for separating and analyzing hydrocarbon components of hydrocarbon fuels”, filed on May 31, 2019 before the Chinese Patent Office; the priority of a patent application No. 201910472985.0, titled “reversible enrichment material for aromatic component in hydrocarbon fuels and preparation thereof”, filed on May 31, 2019 before the Chinese Patent Office; and the priority of a patent application No. 201910472990.1, titled “a packed column and a system for separating and analyzing hydrocarbon components of hydrocarbon fuels”, filed on May 31, 2019 before the Chinese Patent Office, the contents of which are incorporated herein by reference in their entirety.
The present application relates to the field of adsorption materials, particularly to a reversible enrichment material suitable for use in the separation of saturated hydrocarbons from unsaturated hydrocarbons (also referred to as “non-saturated hydrocarbons”), its preparation and application thereof.
Since the hydrocarbon composition of hydrocarbon fuel is closely related to its combustion performance and service performance, and is related to the environmental problems which are increasingly regarded as important, how to optimize the hydrocarbon composition of hydrocarbon fuel, improve the combustion performance thereof, and reduce the emission of harmful substances is a major concern in the petrochemical industry. Currently, the three major refined oil products (gasoline, aviation fuel and diesel oil) have different requirements on the hydrocarbon composition of hydrocarbon fuels due to differences of working principles of engines, working environments and the like; for gasoline, more isoparaffins and less olefins and aromatics are desired, for aviation fuel, more naphthenes is desired, while the content of aromatics should be strictly controlled, and for diesel oil, more n-paraffins and less branched isoparaffins and n-olefins are desired, while the content of polycyclic aromatic hydrocarbons with short side chains should be strictly controlled. Therefore, detailed hydrocarbon composition analysis is of great significance to product quality control of hydrocarbon fuels, related process development and catalyst development.
In current detailed hydrocarbon composition analysis of hydrocarbon fuels, especially aviation fuel and diesel oil, the devices used mainly include standard wall glass tube adsorption column, high performance liquid chromatograph and gas chromatograph-mass spectrometer. The standard wall glass tube adsorption column is used in the fluorescent indicator adsorption method GB/T 11132-2008 (corresponding to ASTM D1319), and its application in the hydrocarbon composition analysis of hydrocarbon fuels involoes the preparation of silica gel for the adsorption column, the filling of the adsorption column, the addition of a color developing agent, the leaching in the separation process, the measurement after the leaching and the like, so that the analysis period is long, the result reproducibility tolerance range is wide, the precision is poor, and this device can only give the content information of saturated hydrocarbon, olefin and aromatic hydrocarbon of the hydrocarbon fuel while cannot give detailed hydrocarbon composition information; the high performance liquid chromatograph is used in SH/T0806-2008 and ASTM D6379-11 and other methods for determining the types of aromatic hydrocarbons of aviation fuel and middle distillate, and when compared with a standard wall glass tube adsorption column, this device has the advantages that the separation speed and the separation efficiency are significantly improved, the content information of saturated hydrocarbon, monocyclic aromatic hydrocarbon and bicyclic aromatic hydrocarbon can be given, but due to the fact that a differential refraction detector is used, the difference responses between different types of aromatic hydrocarbons is large, and thus the quantitative error of different types of aromatic hydrocarbons is large, and detailed hydrocarbon composition of saturated hydrocarbons and olefin information cannot be given.
With the increasing maturity of gas chromatography-mass spectrometry technology, gas chromatograph-mass spectrometer is widely used in the field of petrochemical industry, but due to insufficient capacity of the chromatographic column, online separation and detailed hydrocarbon composition analysis of aviation fuels and middle distillates by gas chromatography-mass spectrometry cannot be realized. This device is used in the SH/T0606-2005 method for the analysis of detailed hydrocarbon composition of hydrocarbon fuels, but in the gas chromatograph-mass spectrometer used in the SH/T0606-2005 method, the chromatographic column in the oven is an empty quartz capillary column which does not have separation capacity, the separation is accomplished by the solid phase extraction separation performed before a sample enters the gas chromatograph-mass spectrometer, where the hydrocarbon fuel is separated into saturated hydrocarbons and aromatic hydrocarbons which then enter the gas chromatograph-mass spectrometer separately for analysis. When using this device, the time for analyzing the detailed hydrocarbon composition of hydrocarbon fuels is long, the olefin component is entrained in the saturated hydrocarbon component during the solid phase extraction separation process, and the gas chromatograph-mass spectrometer cannot distinguish naphthenes from olefins in the hydrocarbon fuel.
There remains an urgent need in the art for new material, device and method suitable for hydrocarbon component separation and analysis of hydrocarbon-based materials, particularly hydrocarbon fuels, containing saturated and unsaturated hydrocarbons.
An object of the present application is to provide a reversible enrichment material suitable for use in the separation of saturated hydrocarbons from unsaturated hydrocarbons, particularly in the separation of aromatic hydrocarbons from saturated hydrocarbons in hydrocarbon fuels, its preparation and application thereof.
To achieve the above object, in an aspect, the present application provides a reversible enrichment material comprising:
an inorganic carrier; and
an active metal salt, a first metal salt promoter and a second metal salt promoter that are supported on the inorganic carrier;
wherein the active metal salt is selected from the group consisting of soluble silver salts, soluble copper salts, or combinations thereof, the first metal salt promoter is one or more selected from the group consisting of soluble salts of Group IA, Group IIA, and Group IIIA metals, and the second metal salt promoter is one or more selected from the group consisting of soluble salts of transition metals other than Group IB metals,
in the reversible enrichment material, based on the total amount of the inorganic carrier, the active metal salt is present in an amount of about 0.1-80% by mass, preferably about 0.5-50% by mass; the first metal salt promoter is present in an amount of about 0.1-80% by mass, preferably about 0.2-40% by mass; the second metal salt promoter is present in an amount of about 0.5-80% by mass, preferably about 0.5-30% by mass.
Preferably, the inorganic carrier has been subjected to a modification comprising sequentially a calcination treatment, an acid-washing and/or alkali-washing treatment and a drying treatment.
In another aspect, the present application provides a method for preparing the reversible enrichment material, comprising the steps of:
1) providing an inorganic carrier;
2) loading the active metal salt, the first metal salt promoter and the second metal salt promoter onto the inorganic carrier; and
3) optionally, drying the material obtained in step 2).
Preferably, the step 1) further comprises subjecting an inorganic starting material to a modification to obtain the inorganic carrier, wherein the modification comprises sequentially a calcination treatment, an acid-washing and/or alkali-washing treatment, and a drying treatment.
In yet another aspect, the present application provides a packed column comprising a column tube and an enrichment filler packed in the column tube, wherein the enrichment filler is a reversible enrichment material according to the present application.
Preferably, the inner surface of the column tube has been subjected to a passivation treatment, and the passivation treatment includes an alkali treatment and an acid treatment.
In yet another aspect, the present application provides a separation and analysis system comprising a packed column according to the present application.
Preferably, the system further comprises a gas chromatograph, wherein the packed column is connected between a sample inlet and a detector of the gas chromatograph.
Preferably, the system further comprises a gas chromatograph-mass spectrometer, wherein the gas chromatograph-mass spectrometer comprises a sample inlet and an analysis module, and the two ends of the packed column are respectively communicated with the sample inlet and an inlet of the analysis module;
the analysis module comprises a mass spectrometry unit and a gas chromatography unit, and inlets of the mass spectrometry unit and the gas chromatography unit are respectively communicated with the inlet of the analysis module through a spilitter.
In yet another aspect, the present application provides a method for performing hydrocarbon component separation and analysis on a hydrocarbon-based material comprising saturated hydrocarbon and unsaturated hydrocarbon, comprising the steps of:
S1) feeding the hydrocarbon-based material into a packed column from a first end thereof by purging with a carrier gas under a first separation condition for enrichment and separation, to obtain a first effluent comprising saturated hydrocarbon from a second end of the packed column;
S2) purging the packed column from the second end thereof with the carrier gas under a second separation condition, to obtain a second effluent comprising unsaturated hydrocarbon from the first end of the packed column;
wherein the packed column is a packed column according to the present application and the temperature of the first separation condition is lower than the temperature of the second separation condition.
Preferably, the method further comprises: S3) after step S1, passing the first effluent to a gas chromatograph and a mass spectrometer to perform separation and analysis on saturated hydrocarbon component in the first effluent; and/or,
S4) after step S2, passing the second effluent to a gas chromatograph and a mass spectrometer to perform separation and analysis on unsaturated hydrocarbon component in the second effluent.
The reversible enrichment material according to the present application has a reversible enrichment capacity for unsaturated hydrocarbons, especially aromatic hydrocarbons, is capable of realizing an effective separation of saturated hydrocarbons from unsaturated hydrocarbons, especially aromatic hydrocarbons, has good saturated hydrocarbon passing capacity and strong unsaturated hydrocarbon enrichment capacity, and thus can be used to realize reversible enrichment of unsaturated hydrocarbon component in hydrocarbon-based materials. The enrichment material can be used for hydrocarbon composition analysis of petroleum products, especially the hydrocarbon composition analysis of aviation fuel and diesel oil, allowing a convenient and quick acquirement of accurate hydrocarbon composition data of the petroleum products.
After being coupled with a gas chromatograph or a gas chromatograph-mass spectrometer, the packed column according to the present application can be used for the online separation of saturated hydrocarbon component from unsaturated hydrocarbon component in hydrocarbon-based materials. The system according to the present application can realize a stable coupling of packed column system and gas chromatograph-mass spectrometer, and therefore can realize an online separation of saturated hydrocarbon and unsaturated hydrocarbon in hydrocarbon-based materials, especially middle distillates such as aviation fuel, diesel oil and the like, improve the repeatability and accuracy of the separation and analysis, accurately provide the olefin and naphthene information of a hydrocarbon fuel, and greatly save the time for detailed hydrocarbon composition analysis of middle distillates such as aviation fuel, diesel oil and the like. The system can be used for quick and accurate determination of detailed hydrocarbon composition of hydrocarbon fuels, especially aviation fuels and diesel oils.
The method according to the present application can realize a quick online separation of saturated hydrocarbon and unsaturated hydrocarbon in hydrocarbon-based materials, especially middle distillates, such as aviation fuel, diesel oil and the like, improve the repeatability, accuracy and efficiency of detailed hydrocarbon composition separation and analysis of hydrocarbon-based materials, solve the problem of existing methods that can not distinguish olefin from naphthene in hydrocarbon-based materials, and greatly save the time for detailed hydrocarbon composition analysis of hydrocarbon-based materials, especially middle distillates such as aviation fuel, diesel oil and the like, while providing more detailed hydrocarbon composition information.
Additional characteristics and advantages of the present application will be described in detail in the Detailed Description section below.
The drawings, forming a part of the present description, are provided to help the understanding of the present application, and should not be considered to be limiting. The present application can be interpreted with reference to the drawings in combination with the detailed description hereinbelow. In the drawings:
The present application will be further described hereinafter in detail with reference to particular embodiments thereof and the accompanying drawings. It should be noted that the particular embodiments of the present application are provided for illustration purpose only, and are not intended to be limiting in any manner.
Any specific numerical value, including the endpoints of a numerical range, described in the context of the present application is not restricted to the exact value thereof, but should be interpreted to further encompass all values close to said exact value. Moreover, regarding any numerical range described herein, arbitrary combinations can be made between the endpoints of the range, between each endpoint and any specific value within the range, or between any two specific values within the range, to provide one or more new numerical range(s), where said new numerical range(s) should also be deemed to have been specifically described in the present application.
Unless otherwise stated, the terms used herein have the same meaning as commonly understood by the person skilled in the art; and if the terms are defined herein and their definitions are different from the ordinary understanding in the art, the definition provided herein shall prevail.
In the context of the present application, in addition to those matters explicitly stated, any matter or matters not mentioned are considered to be the same as those known in the art without any change. Moreover, any of the embodiments described herein can be freely combined with another one or more embodiments described herein, and the technical solutions or ideas thus obtained are considered as part of the original disclosure or original description of the present application, and should not be considered to be a new matter that has not been disclosed or anticipated herein, unless it is clear to the person skilled in the art that such a combination is obviously unreasonable.
All publications, patent applications, patents, and other references cited herein are hereby incorporated by reference in their entirety.
In the present application, the term “hydrocarbon-based material” refers to a material comprising hydrocarbons as a main component, for example, a material having a hydrocarbon content of about 80 wt % or more, preferably about 90 wt % or more, more preferably about 95 wt % or more, especially preferably about 99 wt % or more, and most preferably consisting essentially of hydrocarbons.
In the present application, the term “hydrocarbon fuel” refers to a liquid hydrocarbon-based material typically used in engines, which comprises liquid hydrocarbons having 5 to 25 carbon atoms or mixtures thereof as a main component, and may additionally comprisies a minor amount (e.g., less than about 10 wt %, or less than about 5 wt %) of other materials, such as sulfur-containing compounds.
In the present application, the term “enrichment material” refers to a material that is capable of adsorbing a target component in a multi-component mixture under certain conditions so that the concentration of the target component on said material is higher than that in the bulk phase of the multi-component mixture.
In the present application, the term “reversible” means that the adsorption of the target component by the enrichment material is reversible, i.e. the adsorbed target component can be desorbed from the enrichment material by adjusting the operating conditions, and during the adsorption and desorption process, the type, composition and amount of the target component is essentially unchanged.
In a first aspect, the present application provides a reversible enrichment material suitable for use in the separation of saturated hydrocarbons from unsaturated hydrocarbons, comprising:
an inorganic carrier; and
an active metal salt, a first metal salt promoter and a second metal salt promoter that are supported on the inorganic carrier;
wherein the active metal salt is selected from the group consisting of a soluble silver salt, a soluble copper salt, or a combination thereof, the first metal salt promoter is one or more selected from the group consisting of soluble salts of Group IA, Group IIA and Group IIIA metals, and the second metal salt promoter is one or more selected from the group consisting of soluble salts of transition metals other than Group IB metals.
In a preferred embodiment, the inorganic carrier has been subjected to a modification comprising a calcination treatment, an acid-washing and/or alkali-washing treatment, and a drying treatment performed sequentially.
By loading the active metal salt and two specific types of metal salt promoters on the inorganic carrier, the enrichment material according to the present application can effectively improve the enriching capacity of a single active metal salt on unsaturated hydrocarbons, especially aromatic hydrocarbon component, through the synergistic effect of the metal promoters, and thus is suitable for use in the column for separating saturated hydrocarbon component from unsaturated hydrocarbon component in gas chromatography or gas chromatography-mass spectrometry. Compared with other types of enrichment materials, the reversible enrichment material according to the present application has better passing capacity for saturated hydrocarbons and better enriching capacity for unsaturated hydrocarbons, especially aromatic hydrocarbons. The reversible enrichment material has obvious advantages in passing capacity for saturated hydrocarbons and enriching capacity for low-carbon-number aromatic hydrocarbons in aviation fuel, can stably enrich low-carbon-number aromatic hydrocarbon component (such as ethylbenzene) at a temperature as high as 170° C., has no retainability for long-chain alkane (such as n-hexadecane) in saturated hydrocarbons, can realize a complete separation of saturated hydrocarbons and low-carbon-number aromatic hydrocarbons in aviation fuel, can realize a complete desorption of aromatic hydrocarbons (such as 1-methylnaphthalene) adsorbed by the enrichment material at a temperature of 208° C., can be well used for hydrocarbon composition analysis of aviation fuel, and can improve the accuracy and repeatability of hydrocarbon composition analysis of aviation fuel.
According to the present application, the inorganic carrier may be any porous inorganic material well known to those skilled in the art as a carrier, for example, the inorganic carrier may be one or more selected from the group consisting of diatomite carrier, alumina carrier, titania carrier, zirconia carrier, mesoporous molecular sieve carrier, amorphous silica-alumina carrier, silica gel carrier, and controlled porous glass carrier, preferably a diatomite carrier.
In a preferred embodiment, the inorganic carrier can be obtained by subjecting an inorganic starting material to a modifiaction, for example, by subjecting the inorganic starting material to a calcination treatment, an acid-washing and/or alkali-washing treatment, and a drying treatment sequentially.
In the present application, the inorganic starting materials may be those well known to those skilled in the art and are commercially available, and may be, for example, one or more selected from the group consisting of a diatomite starting material, alumina, titania, zirconia, mesoporous molecular sieves, amorphous silica-alumina, silica gel, and controlled porous glass. According to the application, through the modification, the passing capacity of the inorganic starting material for long-chain alkanes can be improved, so that the performance of the enrichment material for separating saturated hydrocarbons from unsaturated hydrocarbons can be further improved.
In a preferred embodiment, the conditions of the calcination treatment may include: a temperature of about 500-950° C., preferably about 850-950° C., and a period of about 4-16 hours; the conditions of the acid-washing treatment may include: a temperature of about 100-200° C., a period of about 10-40 hours, and a mass ratio of the starting material to be treated on a dry basis to the acid solution of about 1:(1-20), wherein the acid solution used for the acid-washing treatment is one or more selected from the group consisting of nitric acid, hydrochloric acid and sulfuric acid, and the concentration of the acid solution used for the acid-washing treatment is about 1-90% by mass; the conditions of the alkali-washing treatment may include: a temperature of about 100-200° C., a period of about 10-40 hours, and a mass ratio of the starting material to be treated on a dry basis to the alkali solution of about 1:(1-20), wherein the alkali solution used for the alkali-washing treatment is one or more selected from the group consisting of sodium hydroxide solution, potassium hydroxide solution and ammonia water, and the concentration of the alkali solution used for the alkali-washing treatment is about 1-90% by mass, preferably about 10-50% by mass; the conditions of the drying treatment may include: a temperature of about 100-200° C., preferably about 150-180° C., and a period of about 3-6 hours.
In a preferred embodiment, the inorganic carrier may have a specific surface area in a range of from about 1 m2/g to about 600 m2/g, preferably from about 1 m2/g to about 370 m2/g, more preferably from about 1 m2/g to about 100 m2/g, still more preferably from about 2 m2/g to about 50 m2/g, a pore size in a range of from about 1 nm to about 1000 nm, preferably from about 1 nm to about 500 nm, and a particle size in a range of from about 80 μm to about 800 μm, preferably from about 100 μm to about 600 μm.
In a preferred embodiment, based on the total amount of the inorganic carrier, in the reversible enrichment material, the active metal salt may be present in an amount of about 0.1-80% by mass, preferably about 0.5-50% by mass, more preferably about 1-30% by mass or about 0.8-15% by mass; the first metal salt promoter may be present in an amount of about 0.1-80% by mass, preferably about 0.2-40% by mass; the second metal salt promoter may be present in an amount of about 0.5-80% by mass, preferably about 0.5-30% by mass or about 0.7-12% by mass. Further, the ratio of the mass content of the first metal salt promoter to the mass content of the second metal salt promoter, calculated as metal oxide, may be about 1:(0.05-50), for example about 1:(0.05-0.15) or about 1:(0.5-50), preferably about 1:(0.5-40).
In a preferred embodiment, the soluble silver salt may be silver nitrate and the soluble copper salt may be selected from the group consisting of copper nitrate, copper sulfate or a combination thereof, preferably copper nitrate.
In a preferred embodiment, in the first metal salt promoter, the Group IA metal may be one or more selected from the group consisting of lithium, sodium and potassium, the Group IIA metal may be one or more selected from the group consisting of beryllium, magnesium, calcium and barium, the Group IIIA metal may be selected from the group consisting of aluminum, gallium or a combination thereof, and in the second metal salt promoter, the transition metal may be one or more selected from the group consisting of zinc (IIB), cadmium (IIB), vanadium, chromium (VIB), molybdenum (VIB), tungsten (VIB), manganese (VIII), iron (VIII), cobalt (VIII), nickel (VIII), ruthenium (VIII), platinum (VIII), rhodium (VIII) and palladium (VIII). In a further preferred embodiment, the metal salt promoters may be a soluble nitrate or sulphate of the metal promoter.
In a particularly preferred embodiment, the reversible enrichment material comprises one first metal salt promoter and two second metal salt promoters, the first metal salt promoter may be selected from the group consisting of soluble salts of Group IA, Group IIA and Group IIIA metals, preferably from soluble salts of Group IA-IIA metals; the two second metal salt promoters may be selected from the group consisting of soluble salts of transition metals other than Group IB metals. In a further preferred embodiment, the second metal salt promoter may comprise two soluble transition metal salts selected from the group consisting of soluble salts of Group IIB, group VIB and group VIII transition metals, preferably a first soluble transition metal salt selected from soluble salts of Group VIII transition metals and a second soluble transition metal salt selected from soluble salts of Group IIB and Group VIB transition metals. Preferably, the first metal salt promoter may be present in an amount of about 0.1-80% by mass, preferably about 0.2-40% by mass, for example about 0.5-20% by mass or about 0.3-18% by mass, calculated as metal oxide; the two soluble transition metal salts may be present in an amount of about 0.5-80% by mass (preferably about 0.5-30% by mass, for example, about 1.5-22% by mass or about 0.8-16% by mass) and about 0.5-80% by mass (preferably about 0.5-30% by mass, for example, about 1.2-25% by mass or about 0.75-20% by mass), respectively, calculated as metal oxide. Further preferably, the ratio of the mass content of the first soluble transition metal salt to the mass content of the second soluble transition metal salt, calculated as metal oxide, may be about 1:(0.05-40), for example, about 1:(0.05-0.15) or about 1:(0.5-40), preferably about 1:(0.5-30). In a still further preferred embodiment, the first soluble transition metal salt may be selected from soluble salts of Group VIII transition metals and the second soluble transition metal salt may be selected from soluble salts of Group IIB transition metals, wherein the ratio of the mass content of the first soluble transition metal salt to the mass content of the second soluble transition metal salt, calculated as metal oxide, may be about 1:(0.5-30), for example about 1:(0.7-30), about 1:(1.2-26) or about 1:(1.5-25), preferably about 1:(3-20) or about 1:(2.5-15).
In a second aspect, there is provided a method for preparing a reversible enrichment material according to the present application, comprising the steps of:
1) providing an inorganic carrier;
2) loading the active metal salt, the first metal salt promoter and the second metal salt promoter onto the inorganic carrier; and
3) optionally, drying the material obtained in step 2).
In a preferred embodiment, the step 1) may further comprise subjecting an inorganic starting material to a modification to obtain the inorganic carrier, wherein the modification comprises a calcination treatment, an acid-washing and/or alkali-washing treatment, and a drying treatment performed sequentially. The details of the inorganic carrier, the inorganic starting material, and the modification are as described above and are omitted here for brevity.
According to the application, the drying step in the preparation of the reversible enrichment material and the drying treatment in the modification of the inorganic carrier may be the same or different, and can be selected by those skilled in the art in view of the need.
The reversible enrichment material is particularly suitable for use as a filler in a separation column used in gas chromatography analysis of aromatic hydrocarbon content in aviation fuel and detailed hydrocarbon composition analysis of aviation fuel by gas chromatography-mass spectrometry. The enrichment material of the present application can be loaded into a chromatographic column to make a separation chromatographic column required for gas chromatography or gas chromatography-mass spectrometry analysis of the composition of aviation fuel, to separate saturated hydrocarbon component from aromatic hydrocarbon component in aviation fuel, and the separation process may be as follows: after passing through a separation column at a lower temperature, saturated hydrocarbons in the aviation fuel are fed into a gas chromatograph or a gas chromatograph-mass spectrometer for analyzing the components thereof and their contents, and then the temperature of the column box is raised and the separation column is subjected to back flushing, so that aromatic hydrocarbons are fed into the gas chromatograph or gas chromatograph-mass spectrometer for analyzing the components thereof and their contents, so that hydrocarbon composition or detailed hydrocarbon composition analysis data of the aviation fuel is conveniently and quickly obtained.
In a third aspect, the present application provides a packed column suitable for use in the separation of saturated hydrocarbons from unsaturated hydrocarbons, comprising a column tube and an enrichment filler packed in the column tube, wherein the enrichment filler is a reversible enrichment material according to the present application.
The packed column can be stably coupled with a gas chromatograph or a gas chromatograph-mass spectrometer, and allows a full passing of saturated hydrocarbons and a reversible enrichment of unsaturated hydrocarbons in hydrocarbon-based materials, so that an online separation of unsaturated hydrocarbon component from saturated hydrocarbon component in the hydrocarbon-based materials can be realized. The packed column is suitable for use in the online separation of unsaturated hydrocarbons from saturated hydrocarbons in hydrocarbon-based materials, especially hydrocarbon fuels, by gas chromatography or gas chromatography-mass spectrometry, can significantly improve the repeatability and accuracy of hydrocarbon composition analysis and detailed hydrocarbon composition analysis of hydrocarbon fuels, and is simple, convenient and quick to operate.
According to the present application, to avoid the influence of impurities on the surface of the column tube on the analysis result, in a preferred embodiment, the inner surface of the column tube has been subjected to a passivation treatment. Further preferably, the passivation treatment may include an alkali treatment and an acid treatment. For example, the passivation treatment may include: soaking the column tube in an alkali solution having a concentration of 5-20% by mass at 20-100° C. for 30-120 minutes, washing with water to neutrality, soaking in an acid solution having a concentration of 5-20% by mass at 30-120° C. for 30-100 minutes, washing with water to neutrality, and drying.
In a preferred embodiment, the column tube may be U-shaped or spiral-shaped.
In a preferred embodiment, the column tube may have an inner diameter of about 0.1-12 mm, preferably about 1-6 mm, more preferably 1.5-4.5 mm; a length of about 20-5000 mm, preferably about 50-1000 mm, and more preferably 100-600 mm.
In a preferred embodiment, the column tube may be at least one selected from the group consisting of a stainless steel column tube, a glass column tube, and a quartz column tube, and is more preferably a stainless steel column tube.
In a preferred embodiment, the packed column may be used at a temperature ranging from about 80° C. to about 400° C., more preferably from about 100° C. to about 350° C., and even more preferably from about 110° C. to about 300° C.
In a preferred embodiment, the packed column of the present application may be used as a separation column in a gas chromatograph or a gas chromatograph-mass spectrometer, wherein after the separation column is connected in the gas chromatograph or gas chromatograph-mass spectrometer system, a separation experiment of saturated hydrocarbons and unsaturated hydrocarbons in a hydrocarbon-based material is started under a low temperature of the column box; after all of the saturated hydrocarbon component in the hydrocarbon-based material flow out of the separation column, the temperature of the column box is raised and the flow direction of the carrier gas in the separation column is reversed at the same time, and after the temperature is raised to a relatively high temperature, unsaturated hydrocarbon component enriched in the separation column flows out and are fed to an instrument detector for detection, so that the contents of saturated and unsaturated hydrocarbons in the hydrocarbon-based material and detailed hydrocarbon composition information can be conveniently and quickly obtained depending on the type of detector equipped in the instrument.
In a fourth aspect, the present application provides a system suitable for use in hydrocarbon component separation and analysis of a hydrocarbon-based material comprising saturated and unsaturated hydrocarbons, comprising a packed column according to the present application.
In some preferred embodiments, the system may comprise a packed column of the present application and a gas chromatograph, wherein the packed column may be connected between a sample inlet and a detector inlet of the gas chromatograph.
To further analyze the components and their contents in the hydrocarbon component of the hydrocarbon-based material, in other preferred embodiments, the system may further comprise a gas chromatograph-mass spectrometer, which may be of a type commonly used in the art.
In some further preferred embodiments, as shown in
In a further preferred embodiment, to help the maintainance of a vacuum state in the mass spectrometer and ensure a stable coupling of the packed column and the gas chromatograph-mass spectrometer, as shown in
In a further preferred embodiment, to facilitate the control of the purging with the carrier gas and the flow direction of the effluent within the packed column, the system may further comprise a multi-port valve through which the packed column may be switchably coupled to the gas chromatograph-mass spectrometer.
In a further preferred embodiment, as shown in
In the present application, the multi-port valve may be a hand-operated rotary valve and/or a pneumatic rotary valve well known to those skilled in the art that have a plurality of working ports for connecting and controlling multiple pipelines, for example, a six-way valve. The number of the multi-port valves can be one or more. The manner in which the multi-port valve is switched between the first working position and the second working position may be well known to those skilled in the art, for example by turning a handle and/or by pneumatic actuation.
In a particularly preferred embodiment, as shown in
In still further preferred embodiments, as shown in
The packed column and system of the present application may be used for separating and analyzing hydrocarbon components in hydrocarbon-based materials, especially hydrocarbon fuels, which may be at least one of gasoline, aviation fuel and diesel oil, preferably selected from the group consisting of aviation fuel, diesel oil or a combination thereof. The unsaturated hydrocarbon may be selected from the group consisting of aromatic hydrocarbons, olefins, or combinations thereof, preferably aromatic hydrocarbons.
In some preferred embodiments, as shown in
In other preferred embodiments, as shown in
In a fifth aspect, the present application provides a method for performing hydrocarbon component separation and analysis on a hydrocarbon-based material comprising saturated hydrocarbon and unsaturated hydrocarbon, comprising the steps of:
S1) feeding the hydrocarbon-based material into a packed column from a first end thereof by purging with a carrier gas under a first separation condition for enrichment and separation, to obtain a first effluent comprising saturated hydrocarbon from a second end of the packed column; and
S2) purging the packed column from the second end thereof with the carrier gas under a second separation condition, to obtain a second effluent comprising unsaturated hydrocarbon from the first end of the packed column;
wherein the packed column is a packed column according to the present application and the temperature of the first separation condition is lower than the temperature of the second separation condition.
In the method according to the present application, the packed column has a relatively larger enrichment capacity and good releasability for unsaturated hydrocarbons, and can reversibly enrich and release unsaturated hydrocarbons in hydrocarbon-based materials, so that an online separation of unsaturated hydrocarbons from saturated hydrocarbons in hydrocarbon-based materials, especially hydrocarbon fuels, and an accurate determination of detailed hydrocarbon composition thereof can be realized, olefins and naphthenes and the like can be respectively determined qualitatively and quantitatively, the whole process can be performed online, the repeatability and the accuracy of the detailed hydrocarbon composition analysis of hydrocarbon-based materials can be significantly improved, and the time for the detailed hydrocarbon composition analysis of hydrocarbon-based materials can be shortened. This method can be used for quick and accurate determination of detailed hydrocarbon composition of hydrocarbon-based materials, especially hydrocarbon fuels such as aviation fuel and diesel oil, including biomass-derived aviation fuel and biomass-derived diesel oil.
In the method according to the present application, the hydrocarbon-based material may comprise saturated hydrocarbon and unsaturated hydrocarbon, the enrichment material in the packed column can enrich unsaturated hydrocarbon component, the material may adsorb unsaturated hydrocarbon component under the first separation condition, so that saturated hydrocarbon component passes through the packed column, and after all of the saturated hydrocarbon component flows out, the unsaturated hydrocarbon component may be desorbed from the enrichment material under the second separation condition and flows out of the packed column under the action of the carrier gas, so that a separation of the saturated hydrocarbon component from the unsaturated hydrocarbon component can be realized. After all of the saturated hydrocarbon component flows out, to increase the outflow rate of the unsaturated hydrocarbon component, a back flushing with the carrier gas may be performed along a direction opposite to flushing direction under the first separation condition.
In a preferred embodiment, the hydrocarbon-based material is a hydrocarbon fuel, preferably selected from the group consisting of aviation fuel, diesel fuel or a combination thereof; the unsaturated hydrocarbon component is selected from the group consisting of aromatic hydrocarbons, olefins, or combinations thereof, preferably aromatic hydrocarbons.
In the method according to the present application, the first separation condition may vary over a wide range, for example the first separation condition may include: a temperature of about 80-180° C., and a flow rate of the carrier gas of about 1-60 mL/min; to further improve the separation efficiency, it is preferred that the first separation is performed at a temperature of about 115-170° C. and a flow rate of the carrier gas of about 2-45 mL/min; the conditions for the second separation may also vary over a wide range, for example the second separation condition may include: a temperature of about 190-400° C., and a flow rate of the carrier gas of about 1-60 mL/min; further, in order to facilitate the release of the unsaturated hydrocarbon component from the enrichment material and increase the outflow rate, the second separation is preferably performed at a temperature of about 200-350° C. and a carrier gas flow rate of about 2-45 mL/min. Further preferably, the temperature of the second separation condition may differ from the temperature of the first separation condition by about 20-200° C., preferably about 30-100° C.
In a preferred embodiment of the method according to the present application, the first separation condition may be first maintained to perform step S1; when all of the saturated hydrocarbon component flows out under the first separation condition, the temperature may be raised to the second separation condition at a rate that may be, for example, about 10-250° C./min, preferably about 30-150° C./min. Under the first separation condition, to ensure that all of the saturated hydrocarbon component flows out, the first separation condition may be maintained for a time period of, for example, about 1-50 minutes, preferably about 2-30 minutes. Further, after the temperature is raised to the second separation condition, it may be maintained for, for example, about 0.5-10 minutes, preferably about 1-8 minutes, to perform step S2, so as to ensure that all of the unsaturated hydrocarbons flow out.
In the method according to the present application, the carrier gas may be any gas that does not react with the components of the hydrocarbon-based material under the first separation condition and the second separation condition, such as an inert gas, preferably selected from the group consisting of helium, nitrogen, hydrogen, or a combination thereof.
In the method according to the present application, to ensure the efficiency and accuracy of the analysis, the sample amount of the hydrocarbon-based material is preferably about 0.01-2 μL, and more preferably about 0.02-1 μL.
To further analyze the composition of the first and second effluents, in some preferred embodiments, the method may further comprise: S3) after the step S1, passing the first effluent to a gas chromatograph and a mass spectrometer to analyze the kind and content of the saturated hydrocarbon component in the first effluent; and/or S4) after the step S2, passing the second effluent to a gas chromatograph and a mass spectrometer to perform separation and analysis on unsaturated hydrocarbon component in the second effluent.
In a further preferred embodiment, to ensure the analytical accuracy of the gas chromatograph and mass spectrometer, the mass ratio (divide ratio) between the portion of the first effluent entering the gas chromatograph and the portion of the first effluent entering the mass spectrometer may be about (1-40):1, preferably about (5-30):1; the mass ratio between the portion of the second effluent entering the gas chromatograph to the portion of the second effluent entering the mass spectrometer may be about (1-40):1, preferably about (5-30):1.
In the method according to the present application, the operating conditions of the gas chromatography may vary within a wide range, and preferably, the operating conditions of the gas chromatography may include: a temperature of the flame ionization detector of about 200-350° C., preferably about 230-300° C.; operating conditions of the mass spectrometry may include: a temperature of the mass spectrometer transmission line of about 180-400° C., preferably about 200-300° C.
In some preferred embodiments of the method according to the present application, the packed column can be connected between a sample inlet and an analysis module of a gas chromatograph-mass spectrometer to conveniently and quickly perform the method according to the present application using existing gas chromatograph-mass spectrometer; in this embodiment, the hydrocarbon-based material may sequentially pass through the sample inlet, and the packed column for separating out saturated hydrocarbon component and unsaturated hydrocarbon component, which are then fed to the analysis module, respectively, to further analyze the detailed composition thereof.
Further, to facilitate the control of the operation, in some preferred embodiments, the method according to the present application is carried out using a device as shown in
In other preferred embodiments, the method according to the present application is carried out using a device as shown in
In some preferred embodiments, as shown in
In some preferred embodiments, as shown in
In some preferred embodiments, the present application provides the following technical solutions:
A1. A reversible enrichment material for aromatic hydrocarbon component in hydrocarbon fuels, characterized in that the reversible enrichment material comprises: an inorganic carrier; and
an active metal salt, a first metal salt promoter and a second metal salt promoter supported on the inorganic carrier;
wherein the active metal salt is selected from the group consisting of a soluble silver salt, a soluble copper salt, or a combination thereof, the first metal salt promoter is one or more selected from the group consisting of soluble salts of Group IA, Group IIA and Group IIIA metals, and the second metal salt promoter is one or more selected from the group consisting of soluble salts of transition metals other than Group D3 metals;
the inorganic carrier is obtained by subjecting an inorganic starting material to a calcination treatment, an acid-washing and/or alkali-washing treatment and a drying treatment sequentially.
A2. The reversible enrichment material of Item A1, wherein the conditions of the calcination treatment include: a temperature of about 500-950° C. and a period of about 4-16 hours.
A3. The reversible enrichment material of Item A1, wherein the conditions of the acid-washing treatment include: a temperature of about 100-200° C., a period of about 10-40 hours, and a mass ratio of the starting material to be treated on a dry basis to the acid solution of about 1:(1-20), wherein the acid solution used for the acid-washing treatment is one or more selected from the group consisting of nitric acid, hydrochloric acid and sulfuric acid, and the concentration of the acid solution used for the acid-washing treatment is about 1-90% by mass;
the conditions of the alkali-washing treatment include: a temperature of about 100-200° C., a period of about 10-40 hours, and a mass ratio of the starting material to be treated on a dry basis to the alkali solution of about 1:(1-20), wherein the alkali solution used for the alkali-washing treatment is one or more selected from sodium hydroxide solution, potassium hydroxide solution and ammonia water, and the concentration of the alkali solution used for the alkali-washing treatment is about 1-90% by mass.
A4. The reversible enrichment material of Item A1, wherein the conditions of the drying treatment include: a temperature of about 100-200° C. and a period of about 3-6 hours.
A5. The reversible enrichment material of Item A1, wherein the inorganic carrier has a specific surface area of about 1-600 m2/g, a pore size in a range of about 1-1000 nm, and a particle size in a range of about 80-800 μm.
A6. The reversible enrichment material of Item A1 or A5, wherein the inorganic carrier is one or more selected from the group consisting of diatomite carrier, alumina carrier, titania carrier, zirconia carrier, mesoporous molecular sieve carrier, amorphous silica-alumina carrier, silica gel carrier, and controlled porous glass carrier.
A7. The reversible enrichment material of Item A1, wherein, in the reversible enrichment material, the active metal salt is present in an amount of about 0.1-80% by mass, preferably about 0.5-50% by mass; the first metal salt promoter is present in an amount of about 0.1-80% by mass, preferably about 0.2-40% by mass; and the second metal salt promoter is present in an amount of about 0.5-80% by mass, preferably about 0.5-30% by mass.
A8. The reversible enrichment material of Item A1, wherein the ratio of the mass content of the first metal salt promoter to the mass content of the second metal salt promoter, calculated as metal oxide, is about 1:(0.05-0.15) or about 1:(0.5-50).
A9. The reversible enrichment material of Item A1, wherein the soluble silver salt is silver nitrate and the soluble copper salt is selected from the group consisting of copper nitrate, copper sulfate or a combination thereof.
A10. The reversible enrichment material of Item A1, wherein, in the first metal salt promoter, the Group IA metal is one or more selected from the group consisting of lithium, sodium and potassium, the Group IIA metal is one or more selected from the group consisting of beryllium, magnesium, calcium and barium, and the Group IIIA metal is selected from the group consisting of aluminum, gallium or a combination thereof; in the second metal salt promoter, the transition metal is one or more selected from the group consisting of zinc, cadmium, vanadium, chromium, molybdenum, tungsten, manganese, iron, cobalt, nickel, ruthenium, platinum, rhodium and palladium.
A11. The reversible enrichment material of Item A1, wherein the second metal salt promoter comprises two soluble transition metal salts selected from soluble salts of Group VIII transition metals and soluble salts of Group IIB transition metals; the ratio of the mass content of the first soluble transition metal salt to the mass content of the second soluble transition metal salt, calculated as metal oxide, is about 1:(0.05-0.15) or about 1:(0.5-40).
A12. A method for preparing a reversible enrichment material according to any one of Items A1 to A11, characterized in that the method comprises: loading the active metal salt, the first metal salt promoter and the second metal salt promoter onto the inorganic carrier, and then carrying out a drying treatment.
B1. A packed column for reversible enrichment of unsaturated hydrocarbon component in hydrocarbon fuels, characterized in that the packed column comprises a column tube and an enrichment filler filled in the column tube;
the enrichment filler comprises an inorganic carrier, and an active metal salt, a first metal salt promoter and a second metal salt promoter supported on the inorganic carrier;
wherein the active metal salt is selected from the group consisting of soluble silver salts, soluble copper salts, or a combination thereof, the first metal salt promoter is one or more selected from the group consisting of soluble salts of Group IA, Group IIA and Group IIIA metals, and the second metal salt promoter is one or more selected from the group consisting of soluble salts of transition metals other than Group IB metals;
the inorganic carrier is obtained by subjecting an inorganic starting material to a calcination treatment, an acid-washing and/or alkali-washing treatment and a drying treatment sequentially.
B2. The packed column of Item B1, wherein the inorganic carrier is one or more selected from the group consisting of diatomite carrier, alumina carrier, titania carrier, zirconia carrier, mesoporous molecular sieve carrier, amorphous silica-alumina carrier, silica gel carrier, and controlled porous glass carrier.
B3. The packed column of Item B2, wherein the inner surface of the column tube has been subjected to a passivation treatment comprising alkali treatment and acid treatment; and the column tube is a stainless steel column tube, a glass column tube or a quartz column tube.
B4. The packed column of Item B2 or B3, wherein the passivation treatment comprises: soaking the column tube in an alkali solution having a contration of about 5-20% by mass at 20-100° C. for 30-120 minutes, washing with water to neutrality, soaking in an acid solution have a concentration of 5-20% by mass at 30-120° C. for 30-100 minutes, washing with water to neutrality, and drying.
B5. The packed column of Item B1, wherein the column tube is U-shaped or spiral-shaped.
B6. The packed column of Item B1, wherein the column tube has an inner diameter of about 0.1-12 mm and a length of about 20-5000 mm.
B7. The packed column of Item B6, wherein the column tube has an inner diameter of about 1-6 mm and a length of about 50-1000 mm.
B8. The packed column of Item B1, wherein the inorganic carrier has a specific surface area of about 1-600 m2/g, a pore size in a range of about 1-1000 nm, and a particle size in a range of about 80-800 μm.
B9. The packed column of Item B1, wherein, in the enrichment filler, the active metal salt is present in an amount of about 0.1-80% by mass, preferably about 0.5-50% by mass; the first metal salt promoter is present in an amount of about 0.1-80% by mass, preferably about 0.2-40% by mass; and the second metal salt promoter is present in an amount of about 0.5-80% by mass, preferably about 0.5-30% by mass.
B10. the packed column of Item B1, wherein the ratio of the mass contents of the first metal salt promoter to the mass content of the second metal salt promoter, calculated as metal oxide, is about 1:(0.05-0.15) or about 1:(0.5-50).
B11. The packed column of Item B1, wherein the soluble silver salt is silver nitrate and the soluble copper salt is selected from the group consisting of copper nitrate, copper sulfate, or a combination thereof;
in the first metal salt promoter, the Group IA metal is one or more selected from the group consisting of lithium, sodium and potassium, the Group IIA metal is one or more selected from the group consisting of beryllium, magnesium, calcium and barium, and the Group IIIA metal is selected from the group consisting of aluminum, gallium or a combination thereof; in the second metal salt promoter, the transition metal is one or more selected from the group consisting of zinc, cadmium, vanadium, chromium, molybdenum, tungsten, manganese, iron, cobalt, nickel, ruthenium, platinum, rhodium and palladium;
the second metal salt promoter is two selected from the group consisting of soluble salts of transition metals other than Group D3 metals, preferably soluble salts of Group VIII and Group IIB transition metals.
B12. The packed column of Item B10, wherein the second metal salt promoter comprises a first one of the second metal salt promoter selected from soluble salts of Group VIII transition metals and a second one of the second metal salt promoter selected from soluble salts of Group IIB and/or Group VIB transition metals; the ratio of the mass content of the first soluble transition metal salt to the mass content of the second soluble transition metal salt, calculated as metal oxide, is about 1:(0.05-0.15) or about 1:(0.5-40).
B13. The packed column of Item B1, wherein the conditions of the calcination treatment include: a temperature of about 500-950° C. and a period of about 4-16 hours; the conditions of the acid-washing treatment include: a temperature of about 100-200° C., a period of about 10-40 hours, and a mass ratio of the starting material to be treated on a dry basis to the acid solution of about 1:(1-20), wherein the acid solution used for the acid-washing treatment is one or more selected from the group consisting of nitric acid, hydrochloric acid and sulfuric acid, and the concentration of the acid solution used for the acid-washing treatment is about 1-90% by mass;
the conditions of the alkali-washing treatment include: a temperature of about 100-200° C., a period of about 10-40 hours, and a mass ratio of the starting material to be treated on a dry basis to the alkali solution of about 1:(1-20), wherein the alkali solution used for the alkali-washing treatment is one or more selected from the group consisting of sodium hydroxide solution, potassium hydroxide solution and ammonia water, and the concentration of the alkali solution used for the alkali-washing treatment is about 1-90% by mass;
the conditions of the drying treatment include: a temperature of about 100-200° C. and a period of about 3-6 hours.
B14. The packed column of Item B1, wherein the enrichment filler is prepared by a method comprising: loading the active metal salt, the first metal salt promoter and the second metal salt promoter onto the inorganic carrier, and then carrying out a drying treatment.
B15. The packed column of Item B1, wherein the hydrocarbon fuel is selected from the group consisting of aviation fuel, diesel fuel, or a combination thereof; the unsaturated hydrocarbon is selected from aromatic hydrocarbon, olefin, or a combination thereof.
B16. A system for separating and analyzing hydrocarbon components of hydrocarbon fuels, characterized in that the system comprises a packed column according to any one of Items B1 to B15.
B17. The system of Item B16, wherein the system further comprises a gas chromatograph-mass spectrometer; the gas chromatograph-mass spectrometer comprises a sample inlet and an analysis module, wherein two ends of the packed column are respectively communicated with the sample inlet and the inlet of the analysis module;
the analysis module comprises a mass spectrometry unit and a gas chromatography unit, and inlets of the mass spectrometry unit and the gas chromatography unit are respectively communicated with the inlet of the analysis module through a splitter.
B18. The system of Item B17, wherein a first capillary column is connected between the sample inlet and the packed column, and a second capillary column is connected between the packed column and the inlet of the analysis module.
B19. The system of Item B17, wherein the system further comprises a multi-port valve through which the packed column is switchably connected into the gas chromatograph-mass spectrometer.
B20. The system of Item B17, wherein the multi-port valve has a plurality of working ports and has a first working position and a second working position;
in the first working position, the first end of the packed column is communicated with the sample inlet through at least one working port, and the second end of the packed column is communicated with the inlet of the analysis module through at least one working port;
in the second working position, the second end of the packed column is communicated with the sample inlet through at least one working port, and the first end of the packed column is communicated with the inlet of the analysis module through at least one working port.
B21. The system of Item B20, wherein the system further comprises a multi-port valve set comprising a first multi-port valve and a second multi-port valve, the first multi-port valve and the second multi-port valve are connected in a switchable manner, and the packed column is connected into the gas chromatograph-mass spectrometer through the second multi-port valve;
the multi-port valve set has a switch-in working position for connecting the packed column into the system and a switch-out working position for removing the packed column out from the system;
in the switch-in working position, the sample inlet, the first multi-port valve, the packed column connected via the second multi-port valve and the inlet of the analysis module are communicated sequentially;
in the switch-out working position, the packed column is not connected into the system, and the sample inlet, the first multi-port valve, the second multi-port valve and the inlet of the analysis module are communicated sequentially.
B22. The system of Item B20, wherein the multi-port valve is a six-way valve having 6 work ports.
C1. A method for separating and analyzing hydrocarbon components of hydrocarbon fuels, characteried in that the method comprises the steps of:
S1) feeding a hydrocarbon fuel into an enrichment column from a first end thereof under a first separation condition by purging with a carrier gas for enrichment and separation, to obtain a first effluent comprising saturated hydrocarbon from a second end of the enrichment column;
S2) purging the enrichment column from the second end with the carrier gas under a second separation condition, to obtain a second effluent comprising unsaturated hydrocarbon from the first end of the enrichment column;
wherein the temperature of the first separation condition is lower than the temperature of the second separation condition;
the enrichment column comprises a column tube and an enrichment material filled in the column tube; the enrichment material comprises an inorganic carrier, and an active metal salt, a first metal salt promoter and a second metal salt promoter supported on the inorganic carrier; wherein the active metal salt is selected from the group consisting of soluble silver salts, soluble copper salts, or a combination thereof, the first metal salt promoter is one or more selected from the group consisting of soluble salts of Group IA, Group IIA and Group IIIA metals, and the second metal salt promoter is one or more selected from the group consisting of soluble salts of transition metals other than Group IB metals; the inorganic carrier is obtained by subjecting an inorganic starting material to a calcination treatment, an acid-washing and/or alkali-washing treatment and a drying treatment sequentially.
C2. The method of Item C1, wherein the first separation condition include: a temperature of about 80-180° C., and a flow rate of the carrier gas of about 1-60 mL/min; the second separation condition include: a temperature of about 190-400° C., and a flow rate of the carrier gas of about 1-60 mL/min; a difference between the temperature of the second separation condition and the temperature of the first separation condition of about 20-200° C.
C3. The method of Item C1, wherein the method further comprises: maintaining the first separation condition for about 1-50 minutes to perform step S1, and then raising the temperature to about 190-400° C. and maintaining the temperature for about 0.5-10 minutes to perform step S2, wherein the temperature raising rate is about 10-250° C./min.
C4. The method of Item C1, wherein the carrier gas is at least one of helium, nitrogen, and hydrogen.
C5. The method of Item C1, wherein the hydrocarbon fuel is fed in an amount of about 0.01-2 μL.
C6. The method of Item C1, wherein the method further comprises feeding the first effluent to a gas chromatograph and a mass spectrometer to separate and analyze saturated hydrocarbon component therein; and/or, feeding the second effluent to a gas chromatograph and a mass spectrometer to separate and analyze unsaturated hydrocarbon component therein.
C7. The method of Item C1, in which the mass ratio of the first effluent fed into the gas chromatograph and that fed into the mass spectrometer is about (1-40):1; the mass ratio of the second effluent fed into the gas chromatograph and that fed into the mass spectrometer is about (1-40):1.
C8. The method of Item C1, wherein the operating conditions of the gas chromatograph include: a temperature of the flame ionization detector of about 200-350° C.; the operating conditions of the mass spectrometer include: a temperature of the mass spectrometer transmission line of about 180-400° C.
C9. The method of Item C1, wherein the method comprises: connecting the enrichment column between a sample inlet and an analysis module of a gas chromatograph-mass spectrometer; passing the hydrocarbon fuel sequentially through the sample inlet, the reversible enrichment column, and the analysis module.
C10. The method of Item C1, wherein the method further comprises: connecting the enrichment column into a gas chromatograph-mass spectrometer via a multi-port valve configured to have a first working position and a second working position; and
in the first working position, the first end of the enrichment column is communicated with the sample inlet through at least one working port of the multi-port valve, and the second end of the enrichment column is communicated with an inlet of the analysis module through at least one working port, such that at least a portion of the hydrocarbon fuel flows in the enrichment column from the first end to the second end;
in a second working position, the second end of the packed column is communicated with the sample inlet through at least one working port, and an inlet of the enrichment column is communicated with an inlet of the analysis module through at least one working port, such that at least a portion of the hydrocarbon fuel flows in the enrichment column from the second end to the first end;
the method comprises: setting the multi-port valve in the first working position under the first separation condition; and setting the multi-port valve in the second working position under the second separation condition.
C11. The method of Item C1, wherein the method further comprises: connecting the enrichment column into a gas chromatograph-mass spectrometer through a multi-port valve set comprising a first multi-port valve and a second multi-port valve, wherein the multi-port valve set is configured to have a switch-in working position for connecting the enrichment column into the system and a switch-out working position for removing the enrichment column out from the system;
in the switch-in working position, the sample inlet, the first multi-port valve, the enrichment column connected via the second multi-port valve, and an inlet of the analysis module are communicated sequentially so that at least a portion of the hydrocarbon fuel flows through the sample inlet, the first multi-port valve, the enrichment column, and the analysis module sequentially;
in the switch-out working position, the packed column is not connected into the system, and the sample inlet, the first multi-port valve, the second multi-port valve and the inlet of the analysis module are communicated sequentially, so that at least a portion of the hydrocarbon fuel flows through the sample inlet, the first multi-port valve, the second multi-port valve and the analysis module sequentially;
the method comprises: setting the multi-port valve in the switch-in working position under the first and second separation conditions; and setting the multi-port valve in the switch-out working position after the first effluent and the second effluent enter the analysis module for separation and analysis.
C12. The method of Item C1, wherein the method comprises subjecting the column tube to a passivation treatment and then loading the enrichment material into the passivated column tube to obtain the enrichment column; the passivation treatment comprises: soaking the column tube in an alkali solution having a concentration of 5-20% by mass at 20-100° C. for 30-120 minutes, washing with water to neutrality, soaking in an acid solution having a concentration of 5-20% by mass at 30-120° C. for 30-100 minutes, washing with water to neutrality, and then drying;
the column tube is U-shaped or spiral-shaped, the column tube has an inner diameter of about 0.1-12 mm, and a length of about 20-5000 mm; the column tube is at least one of stainless steel column tube, glass column tube and quartz column tube.
C13. The method of Item C1, wherein, in the reversible enrichment material, the active metal salt is present in an amount of about 0.1-80% by mass, preferably about 0.5-50% by mass; the first metal salt promoter is present in an amount of about 0.1-80% by mass, preferably about 0.2-40% by mass; and the second metal salt promoter is present in an amount of about 0.5-80% by mass, preferably about 0.5-30% by mass.
C14. The method of Item C1, wherein the ratio of the mass content of the first metal salt promoter to the mass content of the second metal salt promoter, calculated as metal oxide, is about 1:(0.05-0.15) or 1:(0.5-50).
C15. The method of Item C1, wherein the soluble silver salt is silver nitrate and the soluble copper salt is selected from the group consisting of copper nitrate, copper sulfate, or a combination thereof;
in the first metal salt promoter, the Group IA metal is one or more selected from the group consisting of lithium, sodium and potassium, the Group IIA metal is one or more selected from the group consisting of beryllium, magnesium, calcium and barium, and the Group IIIA metal is selected from the group consisting of aluminum, gallium or a combination thereof; in the second metal salt promoter, the transition metal is one or more selected from the group consisting of zinc, cadmium, vanadium, chromium, molybdenum, tungsten, manganese, iron, cobalt, nickel, ruthenium, platinum, rhodium and palladium;
the second metal salt promoter is two selected from the group consisting of soluble salts of transition metals other than Group D3 metals, preferably soluble salts of Group VIII and Group IIB transition metals.
C16. The method of Item C1, wherein the second metal salt promoter comprises a first one of the second metal salt promoter selected from soluble salts of Group VIII transition metals and a second one of the second metal salt promoter selected from soluble salts of Group IIB and/or group VIB transition metals; the ratio of the mass content of the first soluble transition metal salt to the mass content of the second soluble transition metal salt, calculated as metal oxide, is about 1:(0.05-0.15) or about 1:(0.5-40).
C17. The method of Item C1, wherein the conditions of the calcination treatment include: a temperature of about 500-950° C. and a period of about 4-16 hours;
the conditions of the acid-washing treatment include: a temperature of about 100-200° C., a period of about 10-40 hours, and a mass ratio of the starting material to be treated on a dry basis to the acid solution of about 1:(1-20), wherein the acid solution used for the acid-washing treatment is one or more selected from the group consisting of nitric acid, hydrochloric acid and sulfuric acid, and the concentration of the acid solution used for the acid-washing treatment is about 1-90% by mass;
the conditions of the alkali-washing treatment include: a temperature of about 100-200° C., a period of about 10-40 hours, and a mass ratio of the starting material to be treated on a dry basis to the alkali solution of about 1:(1-20), wherein the alkali solution used for the alkali-washing treatment is one or more selected from the group consisting of sodium hydroxide solution, potassium hydroxide solution and ammonia water, and the concentration of the alkali solution used for the alkali-washing treatment is about 1-90% by mass;
the conditions of the drying treatment include: a temperature of about 100-200° C. and a period of about 3-6 hours.
C18. The method of Item C17, wherein the inorganic carrier is one or more selected from the group consisting of diatomite carrier, alumina carrier, titania carrier, zirconia carrier, mesoporous molecular sieve carrier, amorphous silica-alumina carrier, silica gel carrier, and controlled porous glass carrier; the inorganic carrier has a specific surface area of about 1-600 m2/g, a pore size in a range of about 1-1000 nm, and a particle size in a range of about 80-800 μm.
C19. The method of Item C1, wherein the method further comprises: loading the active metal salt, the first metal salt promoter and the second metal salt promoter onto the inorganic carrier, and then drying to obtain an enrichment material.
C20. The method according to any of Items C1-C19, wherein the hydrocarbon fuel is selected from the group consisting of aviation fuel, diesel fuel, or a combination thereof; the unsaturated hydrocarbon component is selected from aromatic hydrocarbon, olefin, or a combination thereof.
The present application will be further described in detail with reference to examples, but the present application is not limited thereto.
In the following examples and comparative examples, the diatomite starting material was purchased from Suzhou Jiaye Biotechnology Limited, under the trade name Diatomite; other inorganic starting materials were purchased from Sinopharm Chemical Reagent Co., Ltd., unless otherwise stated.
Diatomite starting material and water were mixed at a mass ratio of 1:0.8, slurried and calcined at 850° C. for 8 hours, the calcined diatomite was subjected to an acid-washing treatment for 3 times, wherein the acid used was sulfuric acid, the mass concentration of the acid solution was 20%, the temperature of each acid-washing was 135° C., the time of each acid-washing was 8 hours, and the mass ratio of the diatomite starting material on a dry basis to the acid solution was 1:5, the acid-washed diatomite was filtered, and dried at 150° C. for 3 hours. The contents of each component of the diatomite before and after acid-washing are shown in Table I-1.
The diatomite carrier product obtained was ground and screened for later use, designated as diatomite carrier Z1, which has a pore diameter mainly distributed in a range of 50-1000 nm as measured by mercury intrusion method, and a specific surface area of 13 m2/g as measured by nitrogen physical adsorption method.
Controlled porous glass was calcined at 600° C. for 10 hours, the calcined controlled porous glass was subjected to acid-washing treatment for 1 time, wherein the acid used was nitric acid, the mass concentration of the acid solution was 30%, the temperature of the acid-washing was 150° C., the time of the acid-washing was 10 hours, and the mass ratio of the controlled porous glass starting material on a dry basis to the acid solution was 1:10, the acid-washed controlled porous glass was filtered, and dried at 150° C. for 3 hours.
The controlled porous glass carrier product obtained was screened for later use, designated as controlled porous glass carrier Z2, which has a pore diameter mainly distributed in a range of 2-50 nm as measured by static nitrogen physical adsorption method, and a specific surface area of 367 m2/g as measured by nitrogen physical adsorption method.
Diatomite starting material and water were mixed at a mass ratio of 1:1, slurried and calcined at a high temperature of 950° C. for 15 hours, the calcined diatomite was subjected to alkali-washing treatment for 2 times, wherein the alkali used was sodium hydroxide, the mass concentration of the alkali solution was 15%, the temperature of alkali-washing was 105° C., the time of each alkali-washing was 9 hours, and the mass ratio of the diatomite starting material on a dry basis to the alkali solution was 1:12, the alkali-washed diatomite was filtered, and dried at 120° C. for 3 hours.
The diatomite carrier product obtained was ground and screened for later use, designated as diatomite carrier Z3, which has a pore diameter mainly distributed in a range of 50-1000 nm, and a specific surface area of 9 m2/g as measured by nitrogen physical adsorption method.
Diatomite starting material and water were mixed at a mass ratio of 1:1.5, slurried and calcined at a high temperature of 700° C. for 6 hours, the calcined diatomite was subjected to an acid-washing treatment for 2 times, the acid used was hydrochloric acid, the mass concentration of the acid solution was 5%, the temperature of acid-washing was 110° C., the time of each acid-washing was 3 hours, and the mass ratio of the diatomite starting material on a dry basis to the acid solution was 1:30, the acid-washed diatomite was filtered, and dried at 110° C. for 1.5 hours.
The diatomite carrier product obtained was ground and screened for later use, designated as diatomite carrier Z4, which has a pore diameter mainly distributed in a range of 50-1000 nm, and a specific surface area of 4 m2/g as measured by nitrogen physical adsorption method.
Diatomite starting material and water were mixed at a mass ratio of 1:0.8, slurried and calcined at a high temperature of 850° C. for 8 hours. The calcined diatomite was ground and screened for later use, designated as diatomite carrier D1, which has a pore diameter mainly distributed in a range of 50-1000 nm, and a specific surface area of 2 m2/g as measured by nitrogen physical adsorption method.
Diatomite starting material was subjected to acid-washing treatment for 3 times, wherein the acid used was sulfuric acid, the mass concentration of the acid solution was 20%, the temperature of each acid-washing was 135° C., the time of each acid-washing was 8 hours, and the mass ratio of the diatomite starting material on a dry basis to the acid solution was 1:5, the acid-washed diatomite was filtered, and dried at 150° C. for 3 hours.
The acid-washed diatomite was screened for later use, designated as diatomite carrier D2, which has a pore diameter mainly distributed in a range of 50-1000 nm, and a specific surface area of 3 m2/g as measured by nitrogen physical adsorption method.
The following examples show the effect of the reversible enrichment material of the present application when used in the separation of saturated hydrocarbon and unsaturated hydrocarbon components of hydrocarbon-based materials, in which the reversible enrichment material of the present application was filled in a chromatographic column of a gas chromatograph, and the appearance time of ethylbenzene peak and the time at which n-hexadecane completely flowed out (i.e. completely passed through the chromatographic column) at the temperature for measurement were taken as evaluation criteria, and where the appearance time of ethylbenzene peak was greater than the time at which n-hexadecane completely flowed out at the temperature for measurement, it indicated that the reversible enrichment material had good separation performance.
5.2125 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 10 mL of a solution containing 0.25% by mass of silver nitrate, 0.5% by mass of potassium nitrate and 3% by mass of cadmium nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 0.5%, a mass content of potassium nitrate of 1% and a mass content of cadmium nitrate of 6%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.618 minutes and the appearance time of ethylbenzene peak was 5.336 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.537 minutes and the appearance time of ethylbenzene peak was 3.824 minutes.
5.0525 g of controlled porous glass carrier Z2 with a particle size of 150-400 μm was taken, immersed in 10 mL of a solution containing 0.5% by mass of silver nitrate, 0.5% by mass of gallium nitrate and 10% by mass of palladium nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 1%, a mass content of gallium nitrate of 1% and a mass content of palladium nitrate of 20%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 4.215 minutes and the appearance time of ethylbenzene peak was 5.725 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 3.284 minutes and the appearance time of ethylbenzene peak was 4.307 minutes.
5.0210 g of diatomite carrier Z3 with a particle size of 150-400 μm was taken, immersed in 10 mL solution containing 0.5% by mass of silver nitrate, 5% by mass of beryllium nitrate and 1% by mass of zinc nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 1%, a mass content of beryllium nitrate of 10% and a mass content of zinc nitrate of 2%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.618 minutes and the appearance time of ethylbenzene peak was 5.674 minutes.
5.2100 g of diatomite carrier Z4 with a particle size of 150-400 μm was taken, immersed in 10 mL of a solution containing 0.5% by mass of copper nitrate, 3% by mass of sodium chloride and 1% by mass of nickel nitrate, naturally evaporated to remove water, and then dried in an oven at 100° C. for 1 h to obtain an enrichment material having a mass content of copper nitrate of 1%, a mass content of sodium chloride of 6% and a mass content of nickel nitrate of 2%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.602 minutes and the appearance time of ethylbenzene peak was 6.025 minutes.
6.2564 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 20 mL of a solution containing 1.25% by mass of copper sulfate, 1% by mass of magnesium nitrate and 5% by mass of platinum nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of copper sulfate of 4%, a mass content of magnesium nitrate of 3.2% and a mass content of platinum nitrate of 16%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.602 minutes and the appearance time of ethylbenzene peak was 6.323 minutes.
5.5587g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 20 mL of a solution containing 0.125% by mass of copper nitrate, 2.5% by mass of magnesium nitrate and 0.25% by mass of ferric nitrate, naturally evaporated to remove water, and then dried in an oven at 100° C. for 1 h to obtain an enrichment material having a mass content of copper nitrate of 0.5%, a mass content of magnesium nitrate of 10% and a mass content of ferric nitrate of 1%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph;
when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.602 minutes and the appearance time of ethylbenzene peak was 6.284 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.163 minutes and the appearance time of ethylbenzene peak was 4.821 minutes.
4.9532 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 10 mL of a solution containing 5% by mass of copper nitrate, 10% by mass of potassium nitrate and 2.5% by mass of cobalt nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of copper nitrate of 10%, a mass content of potassium nitrate of 20% and a mass content of cobalt nitrate of 5%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.602 minutes and the appearance time of ethylbenzene peak was 6.886 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.205 minutes and the appearance time of ethylbenzene peak was 4.974 minutes.
4.9865 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 15 mL of a solution containing 5% by mass of copper nitrate, 4% by mass of potassium nitrate, 1% by mass of ferric nitrate and 0.5% by mass of rhodium nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of copper nitrate of 15%, a mass content of potassium nitrate of 12%, a mass content of ferric nitrate of 3% and a mass content of rhodium nitrate of 1.5%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.602 minutes and the appearance time of ethylbenzene peak was 8.897 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.163 minutes and the appearance time of ethylbenzene peak was 5.462 minutes.
4.8765 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 15 mL of a solution containing 10% by mass of silver nitrate, 2% by mass of aluminum nitrate, 5% by mass of cadmium nitrate and 0.5% by mass of ferric nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 30%, a mass content of aluminum nitrate of 6%, a mass content of cadmium nitrate of 15% and a mass content of ferric nitrate of 1.5%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph;
when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.618 minutes and the appearance time of ethylbenzene peak was 9.215 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.257 minutes and the appearance time of ethylbenzene peak was 5.847 minutes.
5.0615 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 20mL of a solution containing 2% by mass of silver nitrate, 1% by mass of lithium nitrate, 3% by mass of ammonium tungstate and 0.2% by mass of ruthenium nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 8%, a mass content of lithium nitrate of 4%, a mass content of ammonium tungstate of 12% and a mass content of ruthenium nitrate of 0.8%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.618 minutes and the appearance time of ethylbenzene peak was 8.867 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.313 minutes and the appearance time of ethylbenzene peak was 4.885 minutes.
10.2684 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 20 mL of a solution containing 2% by mass of silver nitrate, 1% by mass of ferric nitrate, 0.5% by mass of ammonium tungstate and 1% by mass of potassium nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 3.9%, a mass content of ferric nitrate of 1.9%, a mass content of ammonium tungstate of 1.9% and a mass content of potassium nitrate of 1.9%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.467 minutes and the appearance time of ethylbenzene peak was 5.844 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.445 minutes and the appearance time of ethylbenzene peak was 4.157 minutes.
4.8765 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 15 mL of a solution containing 10% by mass of silver nitrate, 2% by mass of aluminum nitrate, 20% by mass of cadmium nitrate and 0.1% by mass of ferric nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 30%, a mass content of aluminum nitrate of 6%, a mass content of cadmium nitrate of 60% and a mass content of ferric nitrate of 0.3%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.341 minutes and the appearance time of ethylbenzene peak was 6.535 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.363 minutes and the appearance time of ethylbenzene peak was 4.031 minutes.
An experiment was conducted substantially as described in Example I-9, except that the diatomite carrier Z1 was replaced with the diatomite carrier Z4.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.704 minutes and the appearance time of ethylbenzene peak was 7.657 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.481 minutes and the appearance time of ethylbenzene peak was 4.882 minutes.
An experiment was conducted substantially as described in Example I-9, except that the diatomite carrier Z1 was replaced with silica gel (produced by Qingdao Haiyang Chemical Co., Ltd.) having a particle size of 150-400 μm specific surface area of 418 m2/g and an average pore diameter of 20.8 nm.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 5.932 minutes and the appearance time of ethylbenzene peak was 6.948 minutes; when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 4.128 minutes and the appearance time of ethylbenzene peak was 4.815 minutes.
An experiment was conducted substantially as described in Example I-9, except that the diatomite carrier Z1 was replaced with γ-Al2O3 having a particle size of 150-400 μm specific surface area of 270 m2/g, and an average pore diameter of 12.1 nm.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 5.027 minutes and the appearance time of ethylbenzene peak was 6.316 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 3.894 minutes and the appearance time of ethylbenzene peak was 4.128 minutes.
An experiment was conducted substantially as described in Example I-9, except that the diatomite support Z1 was replaced with SBA-15 mesoporous molecular sieve having a particle size of 150-400 μm specific surface area of 582 m2/g, and an average pore diameter of 9.8 nm.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 5.276 minutes and the appearance time of ethylbenzene peak was 6.371 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 4.628 minutes and the appearance time of ethylbenzene peak was 5.312 minutes.
An experiment was conducted substantially as described in Example I-9, except that the diatomite carrier Z1 was replaced with zirconia having a particle size of 150-400 μm specific surface area of 92 m2/g and an average pore diameter of 7.8 nm.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 5.034 minutes and the appearance time of ethylbenzene peak was 6.211 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 4.314 minutes and the appearance time of ethylbenzene peak was 4.689 minutes.
An experiment was conducted substantially as described in Example I-9, except that the diatomite carrier Z1 was replaced with the diatomite carrier D1.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 5.315 minutes and the appearance time of ethylbenzene peak was 6.427 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 4.612 minutes and the appearance time of ethylbenzene peak was 4.871 minutes.
An experiment was conducted substantially as described in Example I-9, except that the diatomite carrier Z1 was replaced with the diatomite carrier D2.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.364 minutes and the appearance time of ethylbenzene peak was 4.025 minutes.
An experiment was conducted substantially as described in Example I-9, except that the diatomite carrier Z1 was replaced with an untreated diatomite starting material.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 5.926 minutes and the appearance time of ethylbenzene peak was 6.323 minutes.
This example shows the capacity of the reversible enrichment material of the present application for separating naphthenes from olefins, in which the enrichment material obtained in Example I-9 was filled into a packed column with an inner diameter of 1.6 mm and a length of 300 mm, and the performance in the separation of naphthenes from olefins was evaluated using n-hexane as a solvent, pentylcyclohexane (having a boiling point of 202° C.) as a representative of naphthenes, and 1-octene (having a boiling point of 121° C.) as a representative of light olefins. The chromatographic column was connected into a gas chromatograph, and when measured at a column box temperature of 155° C., the time at which pentylcyclohexane completely flowed out was 0.532 minutes and the appearance time of 1-octene peak was 8.936 minutes. The results show that the material has an excellent performance in the separation of naphthenes from olefins.
5.5362 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 30 mL of a solution containing 4% by mass of silver nitrate and 12% by mass of calcium nitrate, naturally evaporated to remove water, dried in an oven at 150° C. for 1 h, to obtain an enrichment material having a mass content of silver nitrate of 20% and a mass content of calcium nitrate of 60%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.618 minutes and the appearance time of ethylbenzene peak was 3.827 minutes; and when measured at a column box temperature of 170° C., the appearance of ethylbenzene peak was observed before n-hexadecane completely flowed out, which indicated that the separation of n-hexadecane from ethylbenzene failed.
5.7805 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 12 mL of a solution containing 0.5% by mass of silver nitrate and 15% by mass of manganese nitrate, naturally evaporated to remove water, dried in an oven at 150° C. for 1 h, to obtain an enrichment material having a mass content of silver nitrate of 1% and a mass content of manganese nitrate of 30%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.618 minutes and the appearance time of ethylbenzene peak was 3.758 minutes; and the separation of n-hexadecane from ethylbenzene failed at a column box temperature of 170° C.
5.0526 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 10 mL of a solution containing 0.25% by mass of silver nitrate and 1.25% by mass of copper nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 0.5% and a mass content of copper nitrate of 2.5%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph; when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.618 minutes and the appearance time of ethylbenzene peak was 3.855 minutes; and the separation of n-hexadecane from ethylbenzene failed at a column box temperature of 170° C.
5.1527 g of diatomite carrier Z1 with a particle size of 150-400 μm was taken, immersed in 10 mL of a solution containing 0.25% by mass of silver nitrate, 1.25% by mass of chromium nitrate and 0.5% by mass of palladium nitrate, naturally evaporated to remove water, and then dried in an oven at 150° C. for 1 h to obtain an enrichment material having a mass content of silver nitrate of 0.5%, a mass content of chromium nitrate of 2.5% and a mass content of palladium nitrate of 1%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph;
when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.784 minutes and the appearance time of ethylbenzene peak was 5.223 minutes; and when measured at a column box temperature of 170° C., the time at which n-hexadecane completely flowed out was 2.645 minutes and the appearance time of ethylbenzene peak was 3.144 minutes.
5.7943 g of diatomite carrier Z1 with a particle size of 150-400 μm, immersed in 10 mL of a solution containing 1% by mass of potassium nitrate, 3% by mass of ferric nitrate and 0.8% by mass of chromium nitrate, naturally evaporated to remove water, and then dried in an oven at 120° C. for 4 h, to obtain a material having a mass content of potassium nitrate of 1.7%, a mass content of ferric nitrate of 5.2% and a mass content of chromium nitrate of 1.4%, relative to the total amount of the carrier.
The enrichment material obtained was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm, the chromatographic column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the appearance of ethylbenzene peak was observed before the appearance of n-hexadecane peak, which indicated that the material could not retain unsaturated hydrocarbons, and thus could not be used to differentiate saturated hydrocarbons from unsaturated hydrocarbons in a mixture in practical application.
It can be seen from the above examples and comparative examples that, where a same carrier was used, the interaction between the active metal and the metal salt promoter described in the present application can provide the reversible enrichment material obtained with better performance in the separation of saturated hydrocarbons from unsaturated hydrocarbons, and the use of a modified inorganic carrier, especially an inorganic carrier modified by calcining, acid-washing/alkali-washing and drying steps, can further improve the separation performance of the reversible enrichment material obtained.
This example shows the unsaturated hydrocarbon desorption performance of the reversible enrichment material of the present application, in which the enrichment material obtained in Example I-8 was used as a representative example to evaluate the unsaturated hydrocarbon desorption performance.
The enrichment material obtained in Example I-8 was filled into a packed column with an inner diameter of 2 mm and a length of 200 mm to obtain a desired chromatographic column.
Cyclohexane solutions of ethylbenzene, isopropylbenzene, n-butylbenzene, n-pentylbenzene, phenylhexane, n-heptylbenzene, p-di-tert-butylbenzene, 1,3,5 -triisopropylbenzene, tetrahydronaphthalene and 1-methylnaphthalene were respectively formulated as standard samples with mass concentrations of 1%, 2%, 5%, 10%, 8%, 5%, 3%, 2%, 2% and 2% respectively; and a mixed standard sample containing decane, n-undecane, n-dodecane, n-tetradecane, n-pentadecane, n-hexadecane, pentylcyclohexane, hexylcyclohexane, decahydronaphthalene, isopropylbenzene, butylbenzene, tetrahydronaphthalene and 1-methylnaphthalene was formulated, with the mass content of saturated hydrocarbons in the mixed standard sample being 82.9%, and the mass content of unsaturated hydrocarbons in the mixed standard sample being 17.1%.
The chromatographic column obtained was connected into a chromatographic column box, the flow rate of the carrier gas N2 was set to be 25 mL/min, and the initial temperature of the chromatographic column box was set to be 155° C. The sample amount was 0.02 μL, after the cyclohexane completely flowed out of the chromatographic column, the peak area of the cyclohexane peak (ACYH-measured) was measured, then the six-way valve was switched to perform a back flushing of the chromatographic column with the carrier gas, the temperature of the column box was raised to 208° C. at the same time, and the peak area of the unsaturated hydrocarbon peak (AUSH-measured) was measured; and for the mixed standard sample, after hexadecane completely passed through the chromatographic column, the six-way valve was switched to peformed a back flushing with the carrier gas, the temperature of the column box was raised to 208° C. at the same time, to release unsaturated hydrocarbon from the chromatographic column, and the peak areas of the saturated hydrocarbon peak and the unsaturated hydrocarbon peak were measured separately. The mass content of unsaturated hydrocarbon of each standard sample was calculated using normalization method, and compared with the formulation data, to calculate the recovery rate. The results are shown in Table I-2.
As can be seen from the data shown in Table I-2, the unsaturated hydrocarbon desorption performance of the reversible enrichment material of the present application is good, the desorption recovery rate of the material for various unsaturated hydrocarbons after their adsorption is more than 98%, so that a reversible adsorption of unsaturated hydrocarbons, especially aromatic hydrocarbons, can be realized.
The following examples show the preparation of the reversible enrichment material and the packed column of the present application, and the effect thereof in the separation of saturated hydrocarbon and unsaturated hydrocarbon components of hydrocarbon-based materials, in which packed columns filled with the reversible enrichment material of the present application were used in gas chromatograph, and the appearance time of ethylbenzene peak and the time at which n-hexadecane completely flowed out (i.e. completely passed through the chromatographic column) at the temperature for measurement were taken as evaluation criteria, and where the appearance time of ethylbenzene peak was greater than the time at which n-hexadecane completely flowed out at the temperature for measurement, it indicated that the reversible enrichment material and the packed column had good separation performance.
Diatomite starting material was mixed with water, slurried and calcined at a high temperature of 800° C. for 9 hours, the calcined diatomite was subjected to acid-washing treatment for 2 times, the temperature of each acid-washing was 100° C., the time of each acid-washing was 8 hours, the mass ratio of the diatomite starting material on a dry basis to the acid solution was 1:10, the acid used was nitric acid, the mass concentration of the acid solution was 15%, and the acid-washed diatomite was dried at a temperature of 170° C. for 3 hours. The change in the composition of the diatomite before and after the acid-washing treatment is shown in Table II-1.
The diatomite obtained (with a specific surface area of 9 m2/g, and a pore diameter mainly distributed in 50-1000 nm) was ground and screened. 45.2461 g of diatomite with a particle size of 125-630 μm was taken, immersed in 40 mL of a solution containing 4.5% by mass of silver nitrate, 2% by mass of ferric nitrate, 1% by mass of ammonium tungstate and 2% by mass of potassium nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain a reversible enrichment filler having a mass content of silver nitrate of 3.9%, a mass content of ferric nitrate of 1.9%, a mass content of ammonium tungstate of 1% and a mass content of potassium nitrate of 1.9%, relative to the total amount of the carrier.
A U-shaped stainless steel column tube with an inner diameter of 2 mm and a length of 200 mm was subjected to a passivation treatment, in which the tube was soaked in a hot sodium hydroxide solution having a mass concentration of 10% for 30 minutes to remove oil stains on the tube wall, washed with deionised water to neutrality, further treated with a dilute hydrochloric acid aqueous solution having a concentration of 1:20, washed with water to neutrality, and dried for later use.
The enrichment filler obtained was filled into the passivated U-shaped stainless steel column tube with an inner diameter of 2 mm and a length of 200 mm to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.441 minutes and the appearance time of ethylbenzene peak was 5.962 minutes.
Zirconia with a particle size of 125-400 μm was calcined at a high temperature of 650° C. for 8 hours, the calcined zirconia was subjected to an alkali-washing treatment with a sodium hydroxide solution, in which the mass ratio of the zirconia starting material on a dry basis to the alkali solution was 1:20, the mass concentration of the alkali solution was 15%, the temperature of alkali-washing was 140° C., the time of alkali-washing was 20 hours, the alkali-washed zirconia was dried at a temperature of 150° C. for 5 hours.
4.3164 g of the zirconia obtained (with a specific surface area of 120 m2/g, and a pore diameter mainly distributed in 2-20 nm) was taken and immersed in 10 mL of a solution containing 2% by mass of copper nitrate, 1% by mass of potassium nitrate, 1% by mass of nickel nitrate and 2% by mass of chromium nitrate, naturally evaporated to remove water, dired in an oven at 160° C. for 1.5 h to obtain a reversible enrichment filler having a mass content of copper nitrate of 4.5%, a mass content of potassium nitrate of 2.3%, a mass content of nickel nitrate of 2.3% and a mass content of chromium nitrate of 4.5%, relative to the total amount of the carrier.
The enrichment filler obtained was taken, a U-shaped stainless steel column with an inner diameter of 3 mm and a length of 100 mm was passivated as described in Example II-1, the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 2.011 minutes and the appearance time of ethylbenzene peak was 2.997 minutes.
The enrichment filler obtained in Example II-1 was taken, a U-shaped stainless steel column with an inner diameter of 1 mm and a length of 300 mm was passivated as described in Example II-1, the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.582 minutes and the appearance time of ethylbenzene peak was 7.335 minutes.
The enrichment filler obtained in Example II-1 was taken, a U-shaped stainless steel column with an inner diameter of 1 mm and a length of 500 mm was passivated as described in Example II-1, the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 4.795 minutes, and the appearance time of ethylbenzene peak was 8.532 minutes.
The enrichment filler obtained in Example II-1 was taken, a U-shaped stainless steel column with an inner diameter of 1.5 mm and a length of 150 mm was passivated as described in Example II-1, the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed column was connected into a gas chromatograph, and when measured at a column box temperature of 155° C., the time at which n-hexadecane completely flowed out was 2.217 minutes, and the appearance time of ethylbenzene peak was 3.752 minutes.
Diatomite starting material was mixed with water, slurried and calcined at a high temperature of 950° C. for 5 hours, the calcined diatomite was subjected to acid-washing treatment for 2 times, the temperature of each acid-washing was 105° C., the time of each acid-washing was 10 hours, the mass ratio of the diatomite starting material on a dry basis to the acid solution was 1:20, the acid used was hydrochloric acid, the mass concentration of the acid solution was 10%, the acid-washed diatomite was dried at 150° C. for 4 hours.
The diatomite obtained (with a specific surface area of 10 m2/g, and a pore diameter mainly distributed in 50-1000 nm) was ground and screened. 25.2461 g of diatomite with a particle size of 125-400 μm was taken, immersed in 20 ml of a solution containing 2% by mass of silver nitrate, 3% by mass of potassium nitrate, 3% by mass of zinc nitrate and 1% by mass of nickel nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain an enrichment filler having a mass content of silver nitrate of 1.5%, a mass content of potassium nitrate of 2.2%, a mass content of zinc nitrate of 2.2% and a mass content of nickel nitrate of 0.8%, relative to the total amount of the carrier.
A spiral-shaped stainless steel column with an inner diameter of 2 mm and a length of 1000 mm was passivated as described in Example II-1, the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed colume was connected into a gas chromatograph, and when measured at a column box temperature of 160° C., the time at which n-hexadecane completely flowed out was 10.467 minutes and the appearance time of ethylbenzene peak was 15.632 minutes.
The enrichment filler obtained in Example II-6 was taken, a spiral-shaped stainless steel column with an inner diameter of 4 mm and a length of 1200 mm was passivated as described in Example II-1, the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed column was connected into a gas chromatograph, and when measured at a column box temperature of 140° C., the time at which n-hexadecane completely flowed out was 21.598 minutes and the appearance time of ethylbenzene peak was 34.634 minutes.
The diatomite of Example II-6 was ground and sieved, 2.3426 g of diatomite having a particle size of 125-630 μm was taken, immersed in 10 mL of a solution containing 3.5% by mass of copper nitrate, 2.8% by mass of potassium nitrate, 0.7% by mass of iron nitrate and 0.35% by mass of rhodium nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain a reversible enrichment filler having a mass content of copper nitrate of 15%, a mass content of potassium nitrate of 12%, a mass content of iron nitrate of 3% and a mass content of rhodium nitrate of 1.5%, relative to the total amount of the carrier.
The enrichment filler obtained was filled into the stainless steel column tube of Example II-1 to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed column was connted into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.602 minutes and the appearance time of ethylbenzene peak was 8.897 minutes.
The diatomite of Example II-6 was ground and sieved, 2.8863 g of diatomite with a particle size of 125-630 μm was taken, immersed in 10 mL of a solution containing 4% by mass of silver nitrate, 2% by mass of aluminum nitrate, 3% by mass of cadmium nitrate and 1% by mass of ferric nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain a reversible enrichment filler having a mass content of silver nitrate of 14%, a mass content of aluminum nitrate of 7%, a mass content of cadmium nitrate of 10% and a mass content of ferric nitrate of 3.5%, relative to the total amount of the carrier.
The enrichment filler obtained was filled into the stainless steel column tube of Example II-1 to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, the packed column was connted into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 3.692 minutes and the appearance time of ethylbenzene peak was 9.113 minutes.
3.0032 g of silica gel (produced by Qingdao Haiyang Chemical Co., Ltd.) with a particle size of 150-400 μm, specific surface area of 418 m2/g and an average pore diameter of 20.8 nm were taken. The silica gel was immersed in 15 mL of a solution containing 0.1% by mass of silver nitrate and 2.0% by mass of nickel nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain an enrichment filler having a mass content of silver nitrate of 0.5% and a mass content of nickel nitrate of 10%, relative to the total amount of the carrier.
A U-shaped stainless steel column with an inner diameter of 2 mm and a length of 200 mm was passivated as described in Example II-1, the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column, the packed column was connected into a gas chromatograph, and when measured at a column box temperature of 160° C., the time at which n-hexadecane completely flowed out was 3.562 minutes and the appearance time of ethylbenzene peak was 4.036 minutes.
4.256 g of γ-Al2O3 with a particle size of 150-400 μm, specific surface area of 270 m2/g, and an average pore diameter of 12.1 nm was taken. The γ-Al2O3 was immersed in 10 mL of a solution containing 0.5% by mass of silver nitrate and 2.0% by mass of ferric nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain an enrichment filler having a mass content of silver nitrate of 1% and a mass content of ferric nitrate of 4%, relative to the total amount of the carrier.
A U-shaped stainless steel column tube with an inner diameter of 2 mm and a length of 200 mm was passivated as described in Example II-1, the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column, the packed column was connected into a gas chromatograph, and when measured at a column box temperature of 150° C., the time at which n-hexadecane completely flowed out was 4.027 minutes and the appearance time of ethylbenzene peak was 4.536 minutes.
The following Examples II-10 to II-20 show the test results of the packed column of the present application for quantitative analysis of saturated and unsaturated hydrocarbons of hydrocarbon-based materials.
Example II-10
4.893 g of the diatomite obtained in Example II-6 was taken and immersed in 10 mL of a solution containing 0.5% by mass of silver nitrate, 2.0% by mass of chromium nitrate, 1% by mass of palladium nitrate and 1.0% by mass of potassium nitrate, naturally evaporated to remove water, dried in an oven at 150° C. for 1 hour to obtain an enrichment filler having a mass content of silver nitrate of 1%, a mass content of chromium nitrate of 4%, a mass conent of palladium nitrate of 2% and a mass content of potassium nitrate of 2%, relative to the total amount of the carrier.
A U-shaped stainless steel column with an inner diameter of 2 mm and a length of 200 mm was passivated as described in Example II-1, and the enrichment filler obtained was filled into the stainless steel column tube to obtain a packed column for reversible adsorption of unsaturated hydrocarbon, which was connected into a gas chromatograph.
A mixed solution containing decane, n-undecane, n-dodecane, n-tridecane, n-tetradecane, n-pentadecane, hexylcyclohexane, pentylcyclohexane, decahydronaphthalene, isopropylbenzene, butylbenzene, tetrahydronaphthalene and 1-methylnaphthalene was formulated, with the mass content of saturated hydrocarbons being 99.44% and the mass content of unsaturated hydrocarbon being 0.56%. The temperature of the vaporizing chamber was 300° C., the sample amount was 0.02 μL, the initial temperature of the column box was 155° C. and was maintained for 5 minutes, the six-way valve was switched at the time of 5 minutes to conduct a back flushing of the gas circuit in the packed column, the temperature of the column box was raised to 200° C. at a rate of 40° C./min and maintained at 200° C. for 3 minutes. The time at which saturated hydrocarbon completely flowed out was 3 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used. The test conditions were the same as those employed in Example II-10, and the standard solution was formulated using the reagents described in Example II-10, with a difference that the mass content of saturated hydrocarbon in the formulation was 98.26% and the mass content of unsaturated hydrocarbon in the formulation was 1.74%. The time at which saturated hydrocarbon completely flowed out was 3 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used. The test conditions were the same as those employed in Example II-10, and the standard solution was formulated using the reagents described in Example II-10, with a difference that the mass content of saturated hydrocarbon in the formulation was 96.68% and the mass content of unsaturated hydrocarbon in the formulation was 3.32%. The time at which saturated hydrocarbon completely flowed out was 3 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used. The test conditions were the same as those employed in Example II-10, and the standard solution was formulated using the reagents described in Example II-10, with a difference that the mass content of saturated hydrocarbon in the formulation was 94.16% and the mass content of unsaturated hydrocarbon in the formulation was 5.84%. The time at which saturated hydrocarbon completely flowed out was 3 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used. The test conditions were the same as those employed in Example II-10, and the standard solution was formulated using the reagents described in Example II-10, with a difference that the mass content of saturated hydrocarbon in the formulation was 77.26% and the mass content of unsaturated hydrocarbon in the formulation was 22.74%. The time at which saturated hydrocarbon completely flowed out was 3 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used. The test conditions were the same as those employed in Example II-10, and the standard solution was formulated using the reagents described in Example II-10, with a difference that the mass content of saturated hydrocarbon in the formulation was 76.04% and the mass content of unsaturated hydrocarbon in the formulation was 23.96%. The time at which saturated hydrocarbon completely flowed out was 3 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used. The test conditions were the same as those employed in Example II-10, and the standard solution was formulated using the reagents described in Example II-10, with a difference that the mass content of saturated hydrocarbon in the formulation was 72.40% and the mass content of unsaturated hydrocarbon in the formulation was 27.60%. The time at which saturated hydrocarbon completely flowed out was 3 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used. The test conditions were the same as those employed in Example II-10, and the standard solution was formulated using the reagents described in Example II-10, with a difference that the mass content of saturated hydrocarbon in the formulation was 67.32% and the mass content of unsaturated hydrocarbon in the formulation was 32.68%. The time at which saturated hydrocarbon completely flowed out was 3 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used. A mixed solution containing decane, n-undecane, n-dodecane, n-tetradecane, n-hexadecane, hexylcyclohexane, pentylcyclohexane, decahydronaphthalene, isopropylbenzene, butylbenzene, tetrahydronaphthalene and 1-methylnaphthalene was formulated, in which the mass content of saturated hydrocarbon was 82.90%, and the mass content of unsaturated hydrocarbon was 17.10%. The test conditions were the same as those employed in Example II-10, and the time at which saturated hydrocarbon completely flowed out was 4.6 minutes as measured at a carrier gas flow rate of 25 mL/min. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used, and the test conditions were the same as those employed in Example II-10, with a difference that a real aviation fuel sample II-A was used as the test sample, in which the aviation fuel A was an aviation kerosene fraction obtained by hydrotreating straight-run aviation kerosene, which had a distillation range of 160-240° C., and the unsaturated hydrocarbon content of the aviation fuel A measured by a fluorescence chromatographic column is shown in Table II-11. The chromatogram obtained is shown in
The packed column obtained in Example II-10 was used, and the test conditions were the same as those employed in Example II-10, with a difference that a real aviation fuel sample II-B was used as the test sample, in which the aviation fuel sample II-B was an aviation kerosene fraction obtained by hydrocracking a heavy oil, which had a distillation range of 160-280° C., and the unsaturated hydrocarbon content of the aviation fuel sample II-B measured by a fluorescence chromatographic column is shown in Table II-12. The chromatogram obtained is shown in
This example shows the effect of the packed column of the present application in hydrocarbon component analysis of hydrocarbon-based materials, in which the packed column obtained in Example II-10 was used as a representative example to evaluate the performance in hydrocarbon component analysis.
The packed column obtained in Example II-10 was used, and connected into a gas chromatograph-mass spectrometer, an empty capillary column with a length of 30 m and an inner diameter of 0.25 mm was connected between a sample inlet and a six-way valve to buffer the vacuum degree of the system, in which the temperature of the sample inlet was 300° C., and the split ratio of the sample inlet was 20:1. The component flowing out of the packed column was divided into two parts after passing through the splitter, one part entered the flame ionization detector, the other part entered the mass spectrometer, and the split ratio of the two parts was 10:1.
The real aviation fuel sample II-B used in Example II-20 was used as a test sample to perform online separation and detailed analysis of hydrocarbon components of the sample, the mass spectrum and chromatogram obtained are shown in the upper half and the lower half of
Examples II-22 to II-27 are provided to illustrate the system of the present application for separating and analyzing hydrocarbon components of hydrocarbon-based materials and the method of its use.
The device shown in
A mixed solution containing decane, n-undecane, n-dodecane, n-tetradecane, n-hexadecane, hexylcyclohexane, pentylcyclohexane, decahydronaphthalene, dodecene, isopropylbenzene, butylbenzene, tetrahydronaphthalene and 1-methylnaphthalene was formulated, in which the mass content of saturated hydrocarbon was 81.05% and the mass content of unsaturated hydrocarbon was 18.95%.
The solution obtained was used as a test object, the operating conditions of the system for separating and analyzing the hydrocarbon components in the hydrocarbon-based material include: a temperature of dividing/undividing sample inlet of 300° C., a split ratio of 20:1, a carrier gas of helium, a flow rate of 10 mL/min, a temperature of the flame ionization detector of 300° C., and a temperature of the mass spectrometer transmission line of 260° C. The temperature of the valve box was 180° C., the switching time of the six-way valve was 22 minutes, the initial temperature of the column box was 155° C. and maintained for 22 minutes, then the temperature was increased to 206° C. at a rate of 40° C./min and maintained for 3 minutes, and the sample amount was 0.2 μL. The chromatogram obtained is shown in
An experiment was conducted using the device described in Example II-22, with a difference that the embedded packed column had an inner diameter of 2.5 mm and a length of 200 mm, the quartz capillary column 2 had an inner diameter of 0.32 mm and a length of 5 m, the quartz capillary column 5 had an inner diameter of 0.32 mm and a length of 10 m, the quartz capillary column 7 and the quartz capillary column 8 were configured at a split ratio of 10:1, and the enrichment filler used was the enrichment filler of Example II-10.
The device was used to determine the detailed hydrocarbon composition of the solution formulated in Example II-22, and the operating conditions of the system for separating and analyzing hydrocarbon components in the hydrocarbon-based material were the same, except that the six-way valve switching time was 14 minutes and the initial temperature of the column box was maintained for 14 minutes. The chromatogram obtained is shown in
An experiment was conducted using the device described in Example II-22, with a difference that the embedded packed column had an inner diameter of 5 mm and a length of 500 mm, the quartz capillary column 2 had an inner diameter of 0.2 mm and a length of 1 m, the quartz capillary column 5 had an inner diameter of 0.25 mm and a length of 40 m, the quartz capillary column 7 and the quartz capillary column 8 were configured at a split ratio of 15:1, and the enrichment filler used was the enrichment filler of Example II-10.
The device was used to determine the detailed hydrocarbon composition of the solution formulated in Example II-22, and the operating conditions of the system for separating and analyzing hydrocarbon components in the hydrocarbon-based material were the same, except that the six-way valve switching time was 32 minutes and the initial temperature of the column box was maintained for 32 minutes. The chromatogram obtained is shown in
The device shown in
The device was used to determine the detailed hydrocarbon composition of the solution formulated in Example II-22, and the operating conditions of the system for separating and analyzing hydrocarbon components in the hydrocarbon-based material were the same, except that the six-way valve 11 was opened at 0.02 minutes so that the packed column was connected into the gas circuit; the six-way valve 3 was opened at 3.5 minutes so that a back flushing of the gas circuit was realized in the method, the initial temperature of the column box was 155° C. and maintained for 3.5 minutes, and then the temperature was raised to 206° C. at a rate of 40° C./min, and maintained for 2 min; the six-way valve 3 was closed at 6.5 minutes so that the gas flow was restored to the positive direction, and the six-way valve 11 was closed at 6.6 minutes so that the packed column was isolated from the gas circuit of the system; and the sample amount was 0.2 μm. The chromatogram obtained is shown in
The hydrocarbon composition analyzing device used in Example II-25 was used as the experimental equipment, a real aviation kerosene sample II-C was used as a test object, the test conditions were the same as those employed in Example II-25. The chromatogram obtained is shown in
The device for analyzing detailed hydrocarbon composition of the hydrocarbon fuel used in Example II-25 was used as the experimental equipment, and a real diesel oil sample II-D was used as a test object. The operating conditions of the system for separating and analyzing hydrocarbon components of the hydrocarbon-based material were the same as those employed in Example II-25 except that the initial temperature of the column box was 165° C., and the device was used for determining the detailed hydrocarbon composition of the sample II-D, which took 15 minutes. The results of the detailed hydrocarbon composition analysis are shown in Table II-19, in which the measured content is the detailed hydrocarbon composition including that for olefins obtained after the separation of olefins from naphthenes using the packed column of the present application, and the reference content is the detailed hydrocarbon composition determined by conventional mass spectrometry. As can be seen from the comparison of the test results, the system of the present application overcomes the defect of conventional mass spectrometry that it cannot distinguish olefins from naphthenes.
The following examples are provided to illustrate the method of the present application for separating and analyzing hydrocarbon components of hydrocarbon-based materials.
Diatomite starting material was mixed with water, slurried and calcined at a high temperature of 950° C. for 12 hours, the calcined diatomite was subjected to acid-washing treatment for 4 times, the temperature of each acid-washing was 135° C., the time of each acid-washing was 8 hours, the mass ratio of the diatomite starting material on a dry basis to the acid solution was 1:5, the acid used was sulfuric acid, the mass concentration of the acid solution was 30%, the acid-washed diatomite was dried at 120° C. for 4 hours, and the change in the composition of the diatomite before and after treatment is shown in Table III-1.
The diatomite obtained (with a specific surface area of 17 m2/g and a pore diameter mainly distributed in 50-1000 nm) was ground and screened. 24.8532 g of diatomite with a particle size of 125-500 μm was taken, immersed in 20 mL of a solution containing 5.5% by mass of silver nitrate, 3% by mass of ferric nitrate, 1.2% by mass of ammonium tungstate and 3% by mass of potassium nitrate, naturally evaporated to remove water, and dried in an oven at 150° C. for 1 h to obtain an enrichment filler having a mass content of silver nitrate of 4.4%, a mass content of ferric nitrate of 2.4%, a mass content of ammonium tungstate of 1% and a mass content of potassium nitrate of 2.4%, relative to the total amount of the carrier.
A U-shaped stainless steel column tube with an inner diameter of 3 mm and a length of 200 mm was subjected to a passivation treatment, in which the tube was soaked in a hot sodium hydroxide solution having a mass concentration of 10% for 30 minutes to remove oil stains on the tube wall, washed with deionised water to neutrality, further treated with a dilute hydrochloric acid aqueous solution having a concentration of 1:20, washed with water to neutrality, and dried for later use.
The enrichment material obtained was filled into the treated stainless steel column tube to make an enrichment column required for the method, and connected it into the device shown in
The experimental conditions employed in the method include: a temperature of the dividing/undividing sample inlet of 280° C., a split ratio of 20:1, a carrier gas of helium, a flow rate of 10 mL/min, a temperature of the flame ionization detector (FID) of 260° C., and a temperature of the mass spectrometer transmission line of 260° C. The temperature of the valve box was 180° C., the switching time of the six-way valve was 7 minutes, the initial temperature of the column box was 155° C. and maintained for 7 min, then the temperature was increased to 206° C. at a rate of 40° C./min and maintained for 3 minutes, and the sample amount was 0.2 μL.
The formlated sample III-A was used as a test object, and a detailed hydrocarbon composition analysis of the sample III-A was conducted using the method of the present application under the conditions as described above. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the formulated sample are shown in Table III-2, and the results of the detailed hydrocarbon composition analysis are shown in Table III-3.
γ-Al2O3 with a particle size of 150-450 μm was calcined at a high temperature of 500° C. for 5 hours, the calcined γ-Al2O3 was subjected to alkali-washing treatment using a sodium hydroxide solution, the mass ratio of the γ-Al2O3 starting material on a dry basis to the alkali solution was 1:15, the temperature of alkali-washing was 100° C., the time of alkali-washing was 15 hours, the mass concentration of the alkali solution was 5%, and the alkali-washed γ-Al2O3 was dried at 120° C. for 3.5 hours.
3.3542 g of the γ-Al2O3 obtained (with a specific surface area of 261 m2/g, and a pore diameter mainly distributed in 2-50 nm) was taken, immersed in 10 mL of a solution containing 3% by mass of silver nitrate, 1% by mass of lithium nitrate, 2% by mass of manganese nitrate and 0.5% by mass of ferric nitrate, naturally evaporated to remove water, dried in an oven at 125° C. for 3 hours, to obtain a reversible enrichment filler having a mass content of silver nitrate of 9%, a mass content of lithium nitrate of 3%, a mass content of manganese nitrate of 6% and a mass content of ferric nitrate of 1.5%, relative to the total amount of the carrier.
An experiment was conducted using the above-described enrichment filler, using the method described in Example III-1, with a difference that the embedded packed column had an inner diameter of 3.2 mm, a length of 150 mm, the quartz capillary column 2 had an inner diameter of 0.32 mm and a length of 30 m, the quartz capillary column 5 had an inner diameter of 0.32 mm and a length of 1 m, and the quartz capillary column 7 and the quartz capillary column 8 were configured at a split ratio of 6:1.
The experimental conditions employed in the method include: a temperature of the dividing/undividing sample inlet of 280° C., a split ratio of 20:1, a carrier gas of helium, a flow rate of 8 mL/min, a temperature of the flame ionization detector of 260° C., and a temperature of the mass spectrometer transmission line of 260° C. The temperature of the valve box was 180° C., the switching time of the six-way valve was 7.5 minutes, the initial temperature of the column box was 160° C. and maintained for 7.5 minutes, then the temperature was raised to 206° C. at a rate of 40° C./min and maintained for 2 minutes, and the sample amount was 0.2 μL.
The formulated sample III-B was used as a test object, and a detailed hydrocarbon composition analysis of the sample III-B was conducted using the method of the present application under the conditions as described above. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the formulated sample are shown in Table III-4, and the results of the detailed hydrocarbon composition analysis are shown in Table III-5.
The device shown in
The experimental conditions employed in the method include: a temperature of the dividing/undividing sample inlet of 280° C., a split ratio of 20:1, a carrier gas of helium, a flow rate of 10 mL/min, a temperature of the flame ionization detector of 260° C., and a temperature of the mass spectrometer transmission line of 260° C. The temperature of the valve box was 180° C., the six-way valve 11 was opened at 0.02 minutes so that the packed column was connected into the gas circuit; the six-way valve 3 was opened at 14 minutes so that a back flushing of the gas circuit was realized in the method, the initial temperature of the column box was 145° C. and maintained for 14 minutes, then the temperature was raised to 206° C. at a rate of 40° C./min and maintained for 3 min; the six-way valve 3 was closed at 19 minutes so that the gas flow was restored to the positive direction, the six-way valve 11 was closed at 19.1 minutes so that the packed column was isolated from the gas circuit of the system; and the sample amount was 0.2 μL.
The formulated sample III-C was used as a test object, and a detailed hydrocarbon composition analysis of the sample III-C was conducted using the method of the present application under the conditions as described above. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the formulated sample are shown in Table III-6, and the results of the detailed hydrocarbon composition analysis are shown in Table III-7.
An experiment was conducted using the device and enrichment material described in Example III-3, with a difference that the quartz capillary 2 had an inner diameter of 0.32 mm and a length of 5 m, the quartz capillary column 5 had an inner diameter of 0.53 mm and a length of 0.2 m, and the quartz capillary column 7 and the quartz capillary column 8 were configured at a split ratio of 10:1.
The experimental conditions employed in the method include: a temperature of the dividing/undividing sample inlet of 280° C., a split ratio of 20:1, a carrier gas of helium, a flow rate of 10 mL/min, a temperature of the flame ionization detector of 260° C., and a temperature of the mass spectrometer transmission line of 260° C. The temperature of the valve box was 180° C., the six-way valve 11 was opened at 0.02 minutes so that the packed column was connected into the gas circuit; the six-way valve 3 was opened at 14 minutes so that a back flushing of the gas circuit flow was realized in the method, the initial temperature of the column box was 155° C. and maintained for 14 minutes, then the temperature was raised to 206° C. at a rate of 40° C./min and maintained for 3 min; the six-way valve 3 was closed at 19 minutes so that the gas flow was restored to the positive direction, the six-way valve 11 was closed at 19.1 minutes so that the packed column was isolated from the gas circuit of the system; and the sample amount was 0.2 μL.
The formulated sample III-D was used as a test object, and a detailed hydrocarbon composition analysis of the sample III-D was conducted using the method of the present application under the conditions as described above. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the formulated sample are shown in Table III-8, and the results of the detailed hydrocarbon composition analysis are shown in Table III-9.
An experiment was conducted using the method described in Example III-2, with a difference that a real sample III-E was used as a test object, and a detailed hydrocarbon composition analysis of the real sample III-E was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-E obtained are shown in Table III-10, and the results of the detailed hydrocarbon composition analysis are shown in Table III-11, in which the reference data are data obtained using the method described in the reference example.
An experiment was conducted using the method described in Example III-2, with a difference that a real sample III-F was used as a test object, and a detailed hydrocarbon composition analysis of the real sample III-F was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-F obtained are shown in Table III-12, and the results of the hydrocarbon composition analysis are shown in Table III-13, in which the reference data are data obtained using the method described in the reference example.
An experiment was conducted using the method described in Example III-2, with a difference that a real sample III-G was used as a test object, and a detailed hydrocarbon composition analysis of the real sample III-G was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-G obtained are shown in Table III-14, and the results of the detailed hydrocarbon composition analysis are shown in Table III-15, in which the reference data are data obtained using the method described in the reference example.
An experiment was conducted using the method described in Example III-2, with a difference that a real sample III-H was used as a test object, and a detailed hydrocarbon composition analysis of the real sample III-H was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-H obtained are shown in Table III-16, and the results of the detailed hydrocarbon composition analysis are shown in Table III-17, in which the reference data are data obtained using the method described in the reference example.
An experiment was conducted using the method described in Example III-2, with a difference that a real sample III-I was used as a test object, and a detailed hydrocarbon composition analysis of the real sample III-I was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-I obtained are shown in Table III-18, and the results of the detailed hydrocarbon composition analysis are shown in Table III-19, in which the reference data are data obtained using the method described in the reference example.
An experiment was conducted using the method described in Example III-2, with a difference that a real sample III-J were used as a test object, and a detailed hydrocarbon composition analysis of the real sample III-J was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-J obtained are shown in Table III-20, and the results of the detailed hydrocarbon composition analysis are shown in Table III-21, in which the reference data are data obtained using the method described in the reference example.
An experiment was conducted using the method described in Example III-2, with a difference that a real sample III-K was used as a test object, and a detailed hydrocarbon composition analysis of the real sample III-K was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-K obtained are shown in Table III-22, and the results of the detailed hydrocarbon composition analysis are shown in Table III-23, in which the reference data are data obtained using the method described in the reference example.
An experiment was conducted using the method described in Example III-1 with a difference that a biomass aviation fuel sample III-L was used as a test object, the switching time of the six-way valve was 8.5 minutes, and at the moment of 8.5 minutes the temperature of the column box began to raise and was finally raised to 206° C. and maintained for 3 minutes. A detailed hydrocarbon composition analysis of the real sample III-L was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-L obtained are shown in Table III-24, and the results of the detailed hydrocarbon composition analysis are shown in Table III-25, in which the reference data are data obtained using the method described in the reference example.
An experiment was conducted using the method described in Example III-2, with a difference that a real sample III-M was used as a test object, and a detailed hydrocarbon composition analysis of the real sample III-M was conducted using the method of the present application under the conditions as described. The chromatogram obtained is shown in
The results of the total amount of unsaturated and saturated hydrocarbons of the real sample III-M obtained are shown in Table III-26, and the results of the detailed hydrocarbon composition analysis are shown in Table III-27, in which the reference data are data obtained using the method described in the reference example.
The real sample III-E of Example III-5 was used as a representative example, and a detailed hydrocarbon composition analysis of the sample was conducted by using a method comprising sample pre-separation in combination with gas chromatography-mass spectrometry (according to SH/T0606-2005).
5 g of silica gel (with a specific surface area of 300 m2/g, a pore volume of 0.41 mL/g, and a particle size of 75-150 μm) was baked at 150° C. for 3 hours, and 5 g of γ-alumina (with a specific surface area of 240 m2/g, a pore volume of 0.62 mL/g, and a particle size of 75-150 μm) was calcined at 500° C. for 5 hours. The silica gel and the alumina was mixed at a ratio of 95:5 to obtain an adsorbent for the pre-separation of the sample, which was filled into a solid phase extraction column with an inner diameter of 1 cm and a length of 7 cm, and the column was plugged into a sieve plate and was wetted by 1 mL of n-pentane.
100 μL of the sample III-E was taken, placed on the sieve plate holding the solid phase extraction column, eluted with 2 mL of n-pentane, then eluted with 0.5 mL of a mixed solvent of dichloromethane and ethanol (with a volume ratio of 5:1), the effluent obtained being a mixture of saturated hydrocarbon and olefin (hereinafter referred to as saturated hydrocarbon component); and further eluted with 2.5 mL of a mixed solvent of dichloromethane and ethanol (with a volume ratio of 5:1), the effluent obtained being an unsaturated hydrocarbon component; 1 mL of n-triacontane was added using pipettes to the saturated hydrocarbon component and the unsaturated hydrocarbon component, respectively, as an internal standard substance to measure the total amount of the saturated hydrocarbon and the unsaturated hydrocarbon.
The saturated hydrocarbon component and the unsaturated hydrocarbon component obtained by the pre-separation were analyzed using a gas chromatograph-mass spectrometer, respectively, with the analyzing time of each component being 13 minutes. After the spectrums of the saturated hydrocarbon component and the unsaturated hydrocarbon component were collected respectively, and a data analysis was carried out. The whole analysis process took over 30 minutes, and since the olefin component and the saturated hydrocarbon component flowed out together, there was an interference between the analysis of the olefin component and the analysis of the naphthene component, and as a result the olefin component was grouped into the naphthene component. The data of the total amount of the saturated and unsaturated hydrocarbon components of the real sample III-E are shown in Table III-10, and the results of the detailed hydrocarbon composition analysis are shown in Table III-11.
The present application is illustrated in detail hereinabove with reference to preferred embodiments, but is not intended to be limited to those embodiments. Various modifications may be made following the inventive concept of the present application, and these modifications shall be within the scope of the present application.
It should be noted that the various technical features described in the above embodiments may be combined in any suitable manner without contradiction, and in order to avoid unnecessary repetition, various possible combinations are not described in the present application, but such combinations shall also be within the scope of the present application.
In addition, the various embodiments of the present application can be arbitrarily combined as long as the combination does not depart from the spirit of the present application, and such combined embodiments should be considered as the disclosure of the present application.
| Number | Date | Country | Kind |
|---|---|---|---|
| 201910471632.9 | May 2019 | CN | national |
| 201910472985.0 | May 2019 | CN | national |
| 201910472990.1 | May 2019 | CN | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/CN2020/092590 | 5/27/2020 | WO | 00 |
