Patent Application
20180371327
This application claims priority to European application No. 15201135.9—filed on Dec. 18, 2015—, the whole content of this application being incorporated herein by reference for all purposes.
The present invention relates to a process for converting waste plastic into gases, liquid fuels and waxes by catalytic cracking. The process comprises the steps of introducing waste plastic and a catalyst within a reactor; allowing at least a portion of the waste plastic to be converted to gases, liquid fuels, and waxes within the reactor; and removing a product stream containing said gases, liquid fuels and waxes from the reactor.
In view of the increasing importance of polymers as substitutes for conventional materials of construction, such as glass, metal, paper, and wood, the perceived need to save non-renewable resources such as petroleum and dwindling amounts of landfill capacity available for the disposal of waste products, considerable attention has been devoted in recent years to the problem of recovering, reclaiming, recycling or in some way reusing waste plastic.
It has been proposed to pyrolize or catalytically crack the waste plastic so as to convert high molecular weight polymers into volatile compounds having a much lower molecular weight. The volatile compounds, depending on the process employed, can be either relatively high boiling liquid hydrocarbons useful as fuel oils or fuel oil supplements or light to medium boiling hydrocarbons useful as gasoline-type fuels or as other chemicals.
Catalytic cracking of mixed waste plastic is a process well known to the person skilled in the art. For example, U.S. Pat. No. 5,216,149 discloses a method for controlling the pyrolysis of a complex waste stream of plastics to convert such stream into useful high-value monomers or other chemicals, by identifying catalyst and temperature conditions that permit decomposition of a given polymer in the presence of others, without substantial decomposition of the other polymers.
During catalytic cracking, five main families of products are produced: gases, gasoline fraction, kerosene fraction, diesel fraction and waxy compounds. While the latter four may all find existing market applications, the valorization of the former (gases) is harder. This often leads to the utilization of such “off-gas” for energy recovery directly on the production site. For example, U.S. Pat. No. 5,811,606 discloses a method of treating waste hydrocarbon plastics wherein non-condensable components C1-C4 generated from the catalytic cracking in the reactor are collected and sent into the heating furnace to be burnt. Also WO 00/64997 and WO 02/057391 disclose that gaseous hydrocarbon substances are used to heat the thermal cracking reactor.
Further, WO 2012/076890 describes that light hydrocarbons obtained from a hydrocracking reaction chamber can be reintroduced into a dechlorination reaction chamber to act as a hydrogen source for a dechlorination reaction. The authors further disclose that in a process for recycling waste plastic materials optionally non-hydrocracked or partially hydrocracked feedstock from the hydrocracking reaction chamber can be reintroduced into the hydrocracking cracking reactor chamber. However, WO 2012/076890 does not disclose a method for valorization of gases.
In general, it is of advantage to increase the kerosene and diesel fraction since these are valuable products. Further, the quality of diesel fraction obtained should be high, i.e. it should contain a low amount of aromatics.
In the catalytic cracking of waste plastic, high molecular weight polymers are cracked into smaller molecules of lighter weight. In theory, the end product of such cracking reaction mainly consists of gases comprising light weight hydrocarbons. Therefore, a priori, low molecular weight hydrocarbons should not readily react under cracking conditions. If at all, light weight hydrocarbons should undergo reactions which would transform them into even lighter compounds. The present inventors now surprisingly found that contrary to these expectations light weight hydrocarbons being introduced within a reactor for cracking waste plastic are transformed into heavier products thereby increasing the amounts of valuable kerosene and diesel fractions. It was furthermore found that even the undesired gases in the product stream obtained from such cracking reactor can be recycled into the process thereby even further increasing the kerosene and diesel fractions. Additionally, it was found that the additional introduction of light weight hydrocarbons within the cracking reactor yields diesel fractions of higher quality with respect to a decreased amount of aromatics obtained.
The present invention therefore relates to a process for converting waste plastic into gases, liquid fuels and waxes by catalytic cracking, the process comprising:
The one or more C1-4 hydrocarbons introduced within the reactor as additional gas stream can for example be C1-C4 alkanes, C2-4 alkenes and/or C2-4 alkynes. These hydrocarbons may bear substituents, such as hydroxy, amino or halogen. This gas stream may comprise other gases, such as carbon oxide and/or carbon monoxide.
In a preferred embodiment of the process according to the invention the gas stream being additionally introduced within the reactor contains or consists of the gases obtained as “off-gases” from the product stream. Most preferably, the gas stream consists of the off-gases from the product stream. The off-gases may be partly of completely recycled within the process of the present invention.
The gas stream comprising one or more hydrocarbons can be introduced within the reactor prior to, simultaneously with or after the waste plastic.
In the catalytic cracking of plastic several fractions of chemical compounds are obtained. Usually, there is a gas fraction sometimes also referred to as “gases” or “off-gases” containing light weight chemical compounds with less than 5 carbon atoms. The gasoline fraction contains compounds having a low boiling point of for example below 216° C. This fraction includes compounds having 5 to 11 carbon atoms. The kerosene and diesel fraction has a higher boiling point of for example 216° C. to 359° C. This fraction generally contains compounds having 12 to 21 carbon atoms. The even higher boiling fraction is generally designated as wax (Heavy Cycle Oil or HCO). In all the fractions, the compounds are hydrocarbons which optionally comprise heteroatoms, such as N, O, etc. “Liquid fuels” in the sense of the present invention therefore are fuels like gasoline and diesel but may also be used as other valuable chemicals or solvents. “Waxes” designate such hydrocarbons which are solid at room temperature (23° C.) and have a softening point of generally above 45° C.
A plastic is mostly constituted of a particular polymer and the plastic is generally named by this particular polymer. Preferably, a plastic contains more than 25% by weight of its total weight of the particular polymer, preferably more than 40% by weight and more preferably more than 50% by weight. Other components in plastic are for example additives, such as fillers, reinforcers, processing aids, plasticizers, pigments, light stabilizers, lubricants, impact modifiers, antistatic agents, inks, antioxidants, etc. Generally, a plastic comprises more than one additive.
Plastics used in the process of the present invention preferably are polyolefins and polystyrene, such as high density polyethylene (HDPE), low density polyethylene (LDPE), polypropylene (PP) and polystyrene (PS).
Other plastics, such as polyvinylchloride, polyvinylidene chloride, polyethylene terephthalate, polyurethane (PU), acrylonitrile-butadiene-styrene (ABS), nylon and fluorinated polymers are less desirable. If present in the waste plastic, they are preferably present in a minor amount of less than 50% by weight, preferably less than 30% by weight, more preferably less than 20% by weight, even more preferably less than 10% by weight of the total weight of the dry waste plastic. Preferably, the individual content of any less desirable plastic is less than 5% by weight, more preferably less than 2% by weight based on the total weight of the dry waste plastic.
Preferably, the plastics waste starting material comprises one or more thermoplastic polymers and is essentially free of thermosetting polymers. Essentially free in this regard is intended to denote a content of thermosetting polymers of less than 15, preferably less than 10 and even more preferably less than 5 wt % of the composition.
The waste plastic used in the process of the invention may be a single plastic or a mixture of two or more different plastics (mixed waste plastic). Mixed waste plastic being preferred.
Usually, waste plastic contains other non-desired components, namely foreign material, such as paper, glass, stone, metal, etc.
In the context of the present invention whenever it is referred to the weight of the waste plastic or the weight of the polystyrene and polyolefin in the waste plastic, this weight relates to the weight of the dry plastic without any foreign material being admixed with the plastic. However, the weight includes any components in the plastic, such as the above described additives.
The present inventors found that, when a gas stream comprising light weight hydrocarbons is introduced within the reactor, surprisingly the production of valuable products, particularly kerosene and diesel fractions, is increased. This finding is particularly unexpected as such stream should not readily react under cracking conditions. If at all, such gas should undergo reactions which would transform it into even lighter compounds. However, the inventors surprisingly found that, under plastic depolymerization reaction conditions, light hydrocarbons and in particular off-gases are instead transformed into heavier products.
It was furthermore found that in the process of the present invention the diesel quality is improved with respect to an increased concentration of saturated compounds and a decreased concentration of unsaturated compounds, in particular aromatic compounds. At the same time, the also obtained gasoline fraction maintains its high level of quality with respect to Research Octane Number (RON) and Motor Octane Number (MON).
The catalyst used in the process of the present invention may comprise a zeolite-type catalyst. In one embodiment, the catalyst predominantly is a zeolite-type catalyst. In a further embodiment, the catalyst consists of a zeolite-type catalyst. In a third embodiment, the catalyst additionally comprises a further catalyst, in particular an amorphous-type catalyst.
The catalyst used in the process of the present invention may comprise an amorphous-type catalyst. In one embodiment, the catalyst predominantly is an amorphous-type catalyst. In a further embodiment, the catalyst consists of an amorphous-type catalyst. In a third embodiment, the catalyst additionally comprises a further catalyst, in particular a zeolite-type catalyst.
The embodiment in which the catalyst predominantly is a zeolite-type catalyst is preferred. In this context, the term “predominantly” defines a catalyst which is a mixture of a zeolite-type catalyst and a non-zeolite-type catalyst, such as an amorphous catalyst, but wherein the catalyst comprises more than 50% by weight of the zeolite-type catalyst based on the total weight of the catalyst. Preferably, the catalyst comprises more than 60%, more preferably more than 70%, even more preferably more than 80% and most preferably more than 90% of the zeolite-type catalyst. The catalyst can comprise a single zeolite-type catalyst or a mixture of two or more zeolite-type catalysts.
As catalyst all types of FCC catalysts including equilibrated and spent ones may be used. FCC catalysts are well known to the person skilled in the art. For example, the zeolite-type catalyst may be selected from crystalline microporous zeolites which are known to the person skilled in the art and which are commercially available. Preferred examples for zeolite-type catalysts are described in WO 2010/135273, the content of which is incorporated herein by reference. Specific examples for suitable zeolite-type catalysts include but are not limited to ZSM-5, ZSM-11, ZSM-22, ZSM-23, ZSM-35, ZSM-48, ZSM-50, TS-1, TS-2, SSZ-46, MCM-22, MCM-49, FU-9, PSH-3, ITQ-1, EU-1, NU-10, silicalite-1, silicalite-2, boralite-C, boralite-D, BCA, and mixtures thereof.
If the catalyst comprises an amorphous-type catalyst, this may comprise silica, alumina, kaolin, or a mixture thereof. Silica, in particular in the form of sand, is a well known for FCC catalytic applications. Preferred amorphous-type catalysts comprise at least 60% by weight, preferably at least 70% by weight and even more preferably at least 80% by weight of silica-equivalent of an oxidic compound based on silicon like silica (SiO2), kaolin, etc.
The catalyst can be fresh catalyst, equilibrated catalyst (such as spent catalyst), or a mixture thereof.
The waste plastic and the catalyst can be introduced within the reactor simultaneously or subsequently. Furthermore, the mixed waste plastic and the catalyst can be introduced within the reactor batchwise or continuously.
Additionally, the inventors found that the introduction of the gas stream within the cracking reactor opens up new possibilities for the choice of the catalyst for the catalytic cracking reaction. For example, while zeolite-type catalysts and in particular ZSM-5-type catalysts are well known in FCC technology to increase the octane number of the gasoline produced, they have the drawback of leading to higher production of light olefins/gases, which in the prior art were not fully valorized in the plastic catalytic cracking process. Due to the possibility of recycling such gases to the reactor, the present invention makes the appealing addition of for example ZSM-5 now possible.
Finally, the inventors found that the introduction of the gas stream within the cracking reactor and in particular the recycling of off-gases is not detrimental for the reaction kinetics. It was found that the overall conversion is not affected.
The skilled person is aware of suitable apparatus and equipment for carrying out the process in accordance with the present invention and will select the suitable system based on his professional experience, so that no further extensive details need to be given here. However, without willing to be bound to theory, some examples of reactor technologies that can be effectively used to carry out the invention comprise the stirred reactor, the rotary kiln, the bubbling fluidized bed reactor and the circulating fluidized bed reactor riser or downer. The rotary kiln is a cylindrical vessel, inclined slightly to the horizontal, which is rotated slowly about its axis. The material to be processed is fed into the upper end of the cylinder. As the kiln rotates, material gradually moves down towards the lower end, and may undergo a certain amount of stirring and mixing. In a bubbling fluidized bed reactor a fluid (gas or liquid) is passed through the catalyst particles at high enough velocities to suspend the catalyst and cause it to behave as though it were a fluid. In a circulating fluidized bed, also called transport reactor, the catalyst and the fluid flow co-currently at high speed. Generally a cyclone system is used to separate the fluid, which can undergo downstream processing, from the solid, which is recirculated to the reactor. These reactors can be either upflow for risers, or downflow for downers.
Preferably, they are introduced continuously. In one embodiment, the whole process is conducted continuously.
In the reactor, in presence of the catalyst, at least a portion of the mixed waste plastic is converted to gases, liquid fuels and waxes. This conversion preferably takes place at an elevated temperature of for example above 350° C., preferably above 400° C., more preferably above 410° C. Suitably, the conversion takes place at a temperature in the range of above 410° C. to 500° C., more preferably in the range of from 420° C. to 450° C., such as about 425° C.
The effect of introducing the gas stream within the reactor is now explained in more detail with reference to the following examples and the attached figures which show in
In the Figures, in (a) the results of Comparative Example 1 and Example 2, in (b) the results of Comparative Example 3 and Example 4, and in (c) the results of Comparative Example 5 and Example 6 are compared.
The examples below were conducted according to the following general experimental procedure:
In each catalytic run in semibatch mode, 30 g of plastic (20% Polypropylene, 80% Polyethylene) were loaded inside the reactor and a defined amount of catalyst were stored in the catalyst storage tank. The reactor was closed and heated from room temperature to 200° C. during 20 minutes, while simultaneously purging with a 150 mL/min nitrogen flow. When the internal temperature reached the melting point of the plastic, stirring was started and slowly increased to 690 rpm. The temperature was held at 200° C. for 25-30 minutes. During this heating process, nitrogen coming out from the reactor was not collected. Meanwhile, the catalyst storage tank containing the catalyst was purged with nitrogen several times.
After this first pretreatment step and only in those experiments where propylene (C3=) was fed, the flow of nitrogen was decreased from 150 to 103 mL/min and 38 mL/min of propylene are introduced inside the reactor. The flows were allowed to stabilize for several minutes after which the mixture of gases (C3=/N2) was collected in a gas sampling bag for 3 minutes. After this collection of gases, the temperature control set point was changed from external to internal, the internal temperature was increased to the reaction temperature at a heating rate of 10° C./min, and the collection of gases and nitrogen (and C3= if fed) in the corresponding gas sampling bag was started. When the internal temperature reached the reaction temperature, the catalyst was introduced inside the reactor, and the circulation of the gaseous products was commuted to another pair of glass traps and corresponding gas sampling bag. This was considered as the zero reaction time.
During selected time periods, liquid and gaseous products were collected in a pair of glass traps and their associated gas sampling bag, respectively. At the end of the experiment, the flow of propylene (if fed) was stopped and the reactor was cooled to room temperature. During this cooling step, liquids and gases were also collected.
The reaction products were classified into 3 groups: i) gases, ii) liquid hydrocarbons and iii) residue (waxy compounds, ashes and coke accumulated on the catalyst). Quantification of the gases was done by gas chromatography (GC) using nitrogen as the internal standard, while quantification of liquids and residue was done by weight. Glass traps (along with their corresponding caps) were weighed before and after the collection of liquids, while the reactor vessel was weighed before and after each run. For determination of conversion, yields to the different products and composition of gases, the concentration of fed C3= (determined by GC of the first gas sampling bag) was subtracted.
The simulated distillation (SIM-DIS) GC method allowed determination of the different fractions in the liquid samples (according to the selected cuts), the detailed hydrocarbon analysis (DHA) GC method allowed determination of the PIONAU components in the gasoline fraction of the last withdrawn sample (C5-C11: Boiling point <216.1° C.; what included C5-C6 in the gas sample and C5-C11 in the liquid samples), and GC×GC allowed the determination of saturates, mono-, di- and tri-aromatics in the diesel fraction of the last withdrawn liquid samples (C12-C21; 216.1<BP<359° C.).
Should the disclosure of any patents, patent applications, and publications which are incorporated herein by reference conflict with the description of the present application to the extent that it may render a term unclear, the present description shall take precedence.
The experiment was carried out following the general procedure described above. In this example, 20 g of an equilibrated FCC (Fluidized Catalytic Cracking) catalyst ECAT-1C, calcined at 550° C. to remove possible hydrocarbon adsorbed, was used. Reaction temperature was set at 425° C. Propylene was not fed during the reaction. In the attached figures this example is labeled as ECAT-1C.
The experiment was carried out following the general procedure described above. In this example, 20 g of an equilibrated FCC (Fluidized Catalytic Cracking) catalyst ECAT-1C, calcined at 550° C. to remove possible hydrocarbon adsorbed, was used. Reaction temperature was set at 425° C. Propylene was fed during the reaction. In the attached figures this example is labeled as ECAT-1C+C3=.
The experiment was carried out following the general procedure described above. In this example, 20 g of an equilibrated FCC (Fluidized Catalytic Cracking) catalyst, calcined at 550° C. to remove possible hydrocarbon adsorbed, was used. This catalyst was obtained by impregnation of ECAT-1C with a Ga(NO3)3 aqueous solution followed by calcination at 550° C. The amount of Ga(NO3)3 used was calculated in order to obtain 2 wt % Gallium in the final catalyst. Reaction temperature was set at 425° C. Propylene was not fed during the reaction. In the attached figures this example is labeled as 2% Ga-ECAT-1C.
The experiment was carried out following the general procedure described above. In this example, 20 g of an equilibrated FCC (Fluidized Catalytic Cracking) catalyst, calcined at 550° C. to remove possible hydrocarbon adsorbed, was used. This catalyst was obtained by impregnation of ECAT-1C with a Ga(NO3)3 aqueous solution followed by calcination at 550° C. The catalyst contained 2 wt % Gallium. Reaction temperature was set at 425° C. Propylene was fed during the reaction. In the attached figures this example is labeled as 2% Ga-ECAT-1C+C3=.
The experiment was carried out following the general procedure described above. In this example, 20 g of a 92/8 (wt/wt) mixture of an equilibrated FCC (Fluidized Catalytic Cracking) catalyst ECAT-1C and a ZSM-5 based catalyst was used. The ZSM-5 based catalyst was prepared by impregnation of a ZSM-5 catalyst with a Ga(NO3)3 aqueous solution followed by calcination at 550° C. The ZSM-5 based catalyst component contained 3.1 wt % Gallium. The equilibrated catalyst was calcined at 550° C. to remove possible hydrocarbon adsorbed. Reaction temperature was set at 425° C. Propylene was not fed during the reaction. In the attached figures this example is labeled as ECAT-1C+4% Ga CBV5020.
The experiment was carried out following the general procedure described above. In this example, 20 g of a 92/8 (wt/wt) mixture of an equilibrated FCC (Fluidized Catalytic Cracking) catalyst ECAT-1C and a ZSM-5 based catalyst was used. The ZSM-5 based catalyst was prepared by impregnation of a ZSM-5 catalyst with a Ga(NO3)3 aqueous solution followed by calcination at 550° C. The ZSM-5 based catalyst component contained 3.1 wt % Gallium. The equilibrated catalyst was calcined at 550° C. to remove possible hydrocarbon adsorbed. Reaction temperature was set at 425° C. Propylene was fed during the reaction. In the attached figures this example is labeled as ECAT-1C+4% Ga CBV5020+C3=.
The effect of the additional gas stream on the selectivity of the process is shown in
The process of the present invention provides a diesel fraction which comprises a decreased amount of aromatic compounds. This effect is shown in
| Number | Date | Country | Kind |
|---|---|---|---|
| 15201135.9 | Dec 2015 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2016/081295 | 12/15/2016 | WO | 00 |
