Patent Application
20170369797
Syngas (mixtures of hydrogen (H2)) and carbon monoxide (CO) can be readily produced from either coal or methane (natural gas) by methods well known in the art and widely commercially practiced around the world. A number of well-known industrial processes use syngas for producing various oxygenated organic chemicals. The Fischer-Tropsch catalytic process for catalytically producing hydrocarbons from syngas was initially discovered and developed in the 1920's, and was used in South Africa for many years to produce gasoline range hydrocarbons as automotive fuels.
The products produced in a Fischer-Tropsch catalytic process comprise a portion of wax. It is desired to separate the wax from the hydrocarbons in the products so that the hydrocarbons can be further processed in downstream processes.
Accordingly, systems and methods that separate wax from hydrocarbons are disclosed herein.
Disclosed herein is a system comprising: a) a separator tank comprising a first inlet, a second inlet, a first outlet, and a second outlet; b) a heat exchanger; and c) a holding tank comprising a third inlet and a third outlet, wherein the separator tank is in fluid communication with the holding tank via a first connector and via a second connector, wherein the first connector is connected to the first outlet of the separator tank and to the third inlet of the holding tank, wherein the second connector is connected to the first inlet of the separator tank and to the third outlet of the holding tank, and wherein the first connector and the second connector are in communication with the heat exchanger.
Also disclosed herein is a method comprising the steps of: a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product.
Also disclosed herein is a method comprising the steps of: a) providing a first separation liquid comprising a first wax product, wherein the first separation liquid has a second temperature and wherein the first wax product is in liquid or solid form; b) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; c) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and d) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
Also, disclosed herein is a method comprising a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product; c) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; d) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and e) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
Additional advantages will be set forth in part in the description which follows, and in part will be obvious from the description, or can be learned by practice of the aspects described below. The advantages described below will be realized and attained by means of the chemical compositions, methods, and combinations thereof particularly pointed out in the appended claims. It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive.
The accompanying FIGURES, which are incorporated in and constitute a part of this specification, illustrate several aspects, and together with the description, serve to explain the principles of the invention.
Additional advantages of the invention will be set forth in part in the description that follows, and in part will be obvious from the description, or can be learned by practice of the invention. The advantages of the invention will be realized and attained by means of the elements and combinations particularly pointed out in the appended claims. It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the invention, as claimed.
Disclosed herein are materials, compounds, compositions, and components that can be used for, can be used in conjunction with, can be used in preparation for, or are products of the disclosed method and compositions. It is to be understood that when combinations, subsets, interactions, groups, etc. of these materials are disclosed that while specific reference of each various individual and collective combinations and permutation of these compounds cannot be explicitly disclosed, each is specifically contemplated and described herein. For example, if a catalyst component is disclosed and discussed, and a number of alternative solid state forms of that component are discussed, each and every combination and permutation of the catalyst component and the solid state forms that are possible are specifically contemplated unless specifically indicated to the contrary. This concept applies to all aspects of this disclosure including, but not limited to, steps in methods of making and using the disclosed compositions. Thus, if there are a variety of additional steps that can be performed it is understood that each of these additional steps can be performed with any specific aspect or combination of aspects of the disclosed methods, and that each such combination is specifically contemplated and should be considered disclosed.
In this specification and in the claims which follow, reference will be made to a number of terms which shall be defined to have the following meanings:
It must be noted that, as used in the specification and the appended claims, the singular forms “a,” “an” and “the” include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to “a hydrocarbon” includes mixtures of hydrocarbons.
Ranges can be expressed herein as from one particular value, and/or to another particular value. When such a range is expressed, another aspect includes from the one particular value and/or to the other particular value. Similarly, when values are expressed as approximations, by use of the antecedent “,” it will be understood that the particular value forms another aspect. It will be further understood that the endpoints of each of the ranges are significant both in relation to the other endpoint, and independently of the other endpoint.
References in the specification and concluding claims to parts by weight, of a particular element or component in a composition or article, denote the weight relationship between the element or component and any other elements or components in the composition or article for which a part by weight is expressed. Thus, in a compound containing 2 parts by weight of component X and 5 parts by weight of component Y, X and Y are present at a weight ratio of 2:5, and are present in such a ratio regardless of whether additional components are contained in the compound.
A weight percent of a component, unless specifically stated to the contrary, is based on the total weight of the formulation or composition in which the component is included.
As used herein, the terms space time yield (“STY”) refers to the tons or kg of product that is produced per unit time per volume of catalyst.
The Fischer-Tropsch catalytic process for producing hydrocarbons from syngas is known in the art.
The production of wax, CO2, CH4, and heavy hydrocarbon (C10+) is unwanted in Fischer-Tropsch processes, which targets the production of light hydrocarbons (C2-C5). Waxes produced from Fischer-Tropsch processes are typically paraffin waxes, that is, a mixture of hydrocarbon molecules, wherein each molecule contains from 20 to 100 carbon atoms. The systems and methods disclosed herein provide means for separating wax from other hydrocarbons, such as, for example, light hydrocarbons.
Isothermal and/or adiabatic fixed bed reactors can be used to carry out the Fischer-Tropsch process. The isothermal and/or adiabatic fixed bed reactors are used to convert syngas to hydrocarbon products, including, olefins, waxes (e.g. paraffins) and alcohols. The amount of waxes in the hydrocarbon products is less than 5%. In one aspect, the amount of waxes in the hydrocarbon products is less than 4%, 3%, 2%, or 1%.
Disclosed herein is a system comprising: a) a separator tank comprising a first inlet, a second inlet, a first outlet, and a second outlet, b) a heat exchanger, and c) a holding tank comprising a third inlet and a third outlet, wherein the separator tank is in fluid communication with the holding tank via a first connector and via a second connector, wherein the first connector is connected to the first outlet of the separator tank and to the third inlet of the holding tank, wherein the second connector is connected to the first inlet of the separator tank and to the third outlet of the holding tank, and wherein the first connector and the second connector are in communication with the heat exchanger.
In one aspect, the system further comprises a Fisher-Tropsch reactor comprising a fourth inlet and a fourth outlet, wherein the separator tank is in fluid communication with the Fisher-Tropsch via a third connector, wherein the third connector is connected to the to the fourth outlet of the Fisher-Tropsch reactor and the second inlet of the separator tank.
In one aspect, the second connector is in communication with a pump. The pump facilitates the transfer of purified separation fluid from the holding tank to the separator tank.
The heat exchanger serves two purposes. The first purpose is to lower the temperature of the separation liquid comprising a first wax product that is being transported from the separator tank to the holding tank, such lowering the temperature to a second temperature. The temperature of the separation liquid comprising a first wax product can be, for example, lowered from about 140° C. to about 145° C. The second purpose is to increase the temperature of the second separation liquid being transported from the holding tank to a fourth temperature. The fourth temperature can be from about 160° C. to about 190° C.
In one aspect, the third connector is configured to transport a first product gas stream comprising a first wax product and a first lower hydrocarbon product from the Fischer-Tropsch reactor to the separator tank.
In one aspect, the separator tank is configured to withstand at least a pressure of above about 12 bar. For example, the separator tank can be configured to withstand at least a pressure from about 12 bar to about 20 bar.
In one aspect, the separator tank is configured to support a Fischer-Tropsch system on an industrial scale. For example, the separator tank is configured to hold a volume of a first separation fluid on an industrial scale. For example, the holding tank can be configured to hold at least about 1,000 liter of separation fluid. In another example, the holding tank can be configured to have a volume from at least about 1,000 liters to about 20,000 liters.
In one aspect, the first connector is configured to transport a first wax portion and a first separation liquid from the separator tank to the holding tank.
In one aspect, the holding tank is configured to support a Fischer-Tropsch system on an industrial scale. For example, the holding tank is configured to hold a volume of a first separation fluid and a first wax product on an industrial scale. For example, the holding tank can be configured to hold at least about 1,000 liters of separation fluid and wax. In another example, the holding tank can be configured to have a volume from at least about 1,000 liters to about 20,000 liter.
In one aspect, the second connector is configured to transport a second separation liquid from the holding tank to the separator tank.
In one aspect, the separator tank comprises a fifth outlet. The fifth outlet can be connected to a fifth connector that is configured to remove a first lower hydrocarbon product from the separator tank.
In one aspect, the holding tank comprises a sixth outlet. The sixth outlet can be connected to a sixth connector that is configured to remove a first wax product from the holding tank.
Optionally, in various aspects, the disclosed system can be operated or configured on an industrial scale. In one aspect, the system, apparatus, and methods disclosed herein can be configured to produce a first product gas stream comprising a first wax product and a first lower hydrocarbon product on an industrial scale. For example, according to further aspects, the apparatus and methods can separate a first wax product from a first product gas stream comprising a first wax product and a first lower hydrocarbon product in batches on an industrial scale. In a further aspect, the batch size can comprise any desired industrial-scale batch size.
In various aspects, the disclosed system can be operated or performed on any desired time scale or production schedule that is commercially practicable. In one aspect, the disclosed system, apparatus, and methods can produce a quantity of at least 1 ton of a first product gas stream comprising a first wax product and a first lower hydrocarbon product in a period of 2 hr or less, including exemplary quantities of at least about 10 tons within the period. In a further aspect, the period of time can be 1 hr.
In one aspect, the disclosed system, apparatus, and methods can have a STY of at least 0.5/kg/hr of catalyst for the reactors disclosed herein. For example, the disclosed system, apparatus, and methods can have a STY of at least 0.7/kg/hr of catalyst for the reactors disclosed herein. In another example, the disclosed system, apparatus, and methods can have a STY from 0.5 to 1/kg/hr of catalyst for the reactors disclosed herein.
In additional aspects, the components of the disclosed system and apparatus can be shaped and sized to permit production of a first product gas stream comprising a first wax product and a first lower hydrocarbon product on an industrial scale.
Now referring to
The systems disclosed herein can be used in methods to separate wax, such as, for example, paraffins, from a hydrocarbon stream comprising light hydrocarbons.
Disclosed herein is a method comprising the steps of: a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product. In one aspect, the method can further comprise the steps of c) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; d) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and e) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
Also disclosed herein is a method comprising the steps of: a) providing a first separation liquid comprising a first wax product, wherein the first separation liquid has a second temperature and wherein the first wax product is in liquid or solid form; b) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; c) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and d) removing the first wax product from the first separation liquid, thereby producing a second separation liquid. In one aspect, the method further comprises the steps of e) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and f) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with the second separation liquid having the fourth temperature, thereby liquefying or solidifying at least a portion of the first wax product into the second separation, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product. In one aspect, the method further comprises the step of transporting the first separation liquid comprising the first wax product from the holding tank to the heat exchanger.
In one aspect, the step of a) providing a first separation liquid comprising a first wax product, wherein the first separation liquid has a second temperature and wherein the first wax product is in liquid or solid form is performed in a holding tank.
Also, disclosed herein is a method comprising a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product; c) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; d) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and e) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
In one aspect, where appropriate, the second separation liquid can recycled back into step b) and is the first separation liquid. In one aspect, the recycling of the second separation liquid is continuous. In one aspect, the first separation liquid and the second separation liquid being recycled in the separation tank can have a temperature from about 160° C. to about 190° C.
In one aspect, the first temperature is from about 230° C. to about 250° C. For example, the first temperature can be from about 235° C. to about 245° C.
In one aspect, the second temperature is from about 160° C. to about 190° C. For example, the second temperature can be from about 165° C. to about 185° C., such as, from about 170° C. to about 180° C.
In one aspect, the third temperature is from about 140° C. to about 145° C. For example, the third temperature is from about 142° C. to about 144° C.
In one aspect, the fourth temperature is from about 160° C. to about 190° C. For example, the fourth temperature can be from about 165° C. to about 185° C., such as, from about 170° C. to about 180° C.
In one aspect, the first product gas stream comprises less than 5% of the first wax product. For example, the first product gas stream can comprise less than 3% of the first wax product. In another example, first product gas stream can comprise less than 2% of the first wax product. In one aspect, the first product gas stream comprises from about 1% to about 5% of the first wax product.
In one aspect, the second product gas stream comprises less than 0.5% of the first wax product. For example, the second product gas stream can comprise less than 0.3% of the first wax product. In another example, the second product gas stream can comprise less than 0.1% of the first wax product. In one aspect, the second product gas stream comprises from about 0.01% to 0.5% of the first wax product.
In one aspect, at least 50% of the first wax product is separated from the first product gas stream. For example, at least 70% of the first wax product is separated from the first product gas stream. In another example, at least 80% of the first wax product can be separated from the first product gas stream. In yet another example, at least 85% of the first wax product can be separated from the first product gas stream. In another example, at least 90% of the first wax product can be separated from the first product gas stream. In another example, at least 95% of the first wax product can be separated from the first product gas stream. In another example, at least 97% of the first wax product can be separated from the first product gas stream. In another example, at least 99% of the first wax product can be separated from the first product gas stream.
In one aspect, the first product gas stream comprises from about 50% to about 99% of the first lower hydrocarbon product. For example, the first product gas stream can comprise from about 50% to about 90% of the first lower hydrocarbon product. In another example, the first product gas stream can comprise from about 60% to about 80% of the first lower hydrocarbon product.
In one aspect, the first hydrocarbon product comprises C2-C5 hydrocarbons.
In one aspect, the first separation liquid comprises silicone oil, an ionic liquid, or a glycol, or a combination thereof. For example, the first separation liquid can comprise silicone oil. In another example, the first separation liquid can comprise an ionic liquid, such as ioniq liquids of silver and copper salts, such as for example, silver tetrafluoroborate. In yet another example, the first separation liquid can comprise a glycol. The glycol can be a mono, di, or tri glycol compounds. Non-limiting examples of suitable glycols include ethylene glycol, propylene glycol, and 1,3, butanediol. The first separation liquid can be selected to be a liquid that is inert to the first product gas stream and has a boiling point above that of the temperature, such as about 160° C. to about 190° C., during operating pressure conditions of the separator tank. The operating pressure of the separator tank can be from about 3 bar to about 12 bar.
In one aspect, the second separation liquid comprises less than 0.5% of the first wax product. For example, the second separation liquid can comprise less than 0.3% of the first wax product. In another example, the second separation liquid can comprise less than 0.1% of the first wax product. In another example, the second separation liquid can comprise less than 0.05% of the first wax product. In one aspect, the second separation liquid comprises from about 0.01% to 0.5% of the first wax product.
In one aspect, the second separation liquid is substantially identical to the first separation liquid. For example, the second separation can be the first separation liquid.
In one aspect, the separating at least a portion of the first wax product from the first product gas stream is performed in a separator tank at a pressure from about 3 bar to about 12 bar. For example, the separating at least a portion of the first wax product from the first product gas stream is performed in a separator tank at a pressure from about 5 bar to about 10 bar.
In one aspect, the first product gas stream comprises less than 10% of C6+ hydrocarbons. For example, the first product gas stream comprises less than 8% of C6+ hydrocarbons. In another aspect, the first product gas stream comprises less than 5% of C6+ hydrocarbons. In yet another aspect, the first product gas stream comprises from about 1% to about 10% of C6+ hydrocarbons.
In one aspect, the first wax product is in solid form when separated from the first gas product stream. In another aspect, the first wax product is in liquid form when separated from the first gas product stream.
In one aspect, the step of removing the first wax product from the first separation liquid comprises scrapping or skimming the first wax product from the first separation liquid.
In one aspect, the method further comprises transporting the second separation liquid having the fourth temperature to a separator tank.
In view of the described catalyst and catalyst compositions and methods and variations thereof, herein below are described certain more particularly described aspects of the inventions. These particularly recited aspects should not however be interpreted to have any limiting effect on any different claims containing different or more general teachings described herein, or that the “particular” aspects are somehow limited in some way other than the inherent meanings of the language and formulas literally used therein.
Aspect 1: A method comprising the steps of: a) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and b) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with a first separation liquid having a second temperature, thereby liquefying or solidifying at least a portion of the first wax product into the first separation liquid, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product.
Aspect 2: The method of aspect 1, wherein the method further comprises the steps of: c) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; d) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and e) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
Aspect 3: The method of aspect 2, wherein the second separation liquid is recycled back into step b) and is the first separation liquid.
Aspect 4: The method of any one of aspects 1-3, wherein the first temperature is from about 230° C. to about 250° C.
Aspect 5: The method of any one of aspects 1-4, wherein the second temperature is from about 160° C. to about 190° C.
Aspect 6: The method of any one of aspects 2-5, wherein the third temperature is from about 140° C. to about 145° C.
Aspect 7: The method of any one of aspects 1-6, wherein the first product gas stream comprising less than 5% of the first wax product.
Aspect 8: The method of any one of aspects 1-7, wherein the second product gas stream comprising less than 0.5% of the first wax product.
Aspect 9: The method of any one of aspects 1-7, wherein the first product gas stream comprising from about 50% to about 99.5% of the first lower hydrocarbon product.
Aspect 10: The method of any one of aspects 1-9, wherein at least 50% of the first wax product is separated from the first product gas stream.
Aspect 11: The method of any one of aspects 1-9, wherein at least 80% of the first wax product is separated from the first product gas stream.
Aspect 12: The method of any one of aspects 1-9, wherein at least 90% of the first wax product is separated from the first product gas stream.
Aspect 13: The method of any one of aspects 1-12, wherein the first hydrocarbon product comprises C2-C5 hydrocarbons.
Aspect 14: The method of any one of aspects 1-12, wherein the first separation liquid comprises silicone oil, an ionic liquid, or a glycol, or a combination thereof.
Aspect 15: The method of any one of aspects 1-14, wherein the second separation liquid comprises less than 0.5% of the first wax product.
Aspect 16: The method of any one of aspects 1-15, wherein the second separation liquid is substantially identical to the first separation liquid.
Aspect 17: The method of any one of aspects 1-16, wherein the separating at least a portion of the first wax product from the first product gas stream is performed in a separator tank at a pressure from about 3 bar to about 12 bar.
Aspect 18: The method of any one of aspects 1-18, wherein the first product gas stream comprises less than 10% of C10+ hydrocarbons.
Aspect 19: A method comprising the steps of: a) providing a first separation liquid comprising a first wax product, wherein the first separation liquid has a second temperature and wherein the first wax product is in liquid or solid form; b) lowering the second temperature of the first separation liquid to a third temperature by use of a heat exchanger; c) transporting the first separation liquid to a holding tank and allowing the first wax product to float to the surface of the first separation liquid; and d) removing the first wax product from the first separation liquid, thereby producing a second separation liquid.
Aspect 20: The method of aspect 19, wherein the first separation liquid comprises at least 10% of the first wax product.
Aspect 21: The method of aspects 19 or 20, wherein the second temperature is from about 160° C. to about 190° C.
Aspect 22: The method of any one of aspects 19-21, wherein the third temperature is from about 140° C. to about 145° C.
Aspect 23: The method of any one of aspects 19-22, wherein step a) is performed in a holding tank.
Aspect 24: The method of aspect 23, wherein the method further comprises the step of transporting the first separation liquid comprising the first wax product from the holding tank to the heat exchanger.
Aspect 25: The method of any one of aspects 19-24, wherein the first wax product is in solid form.
Aspect 26: The method of any one of aspects 19-25, wherein removing the first wax product from the first separation liquid comprises scrapping or skimming the first wax product from the first separation liquid.
Aspect 27: The method of any one of aspects 19-26, wherein the second separation liquid comprises less than 0.5% of the first wax product.
Aspect 28: The method of any one of aspects 19-27, wherein the method further comprises the step of transporting the second separation liquid to a heat exchanger and increasing the temperature of the second separation liquid to a fourth temperature.
Aspect 29: The method of aspect 28, wherein the fourth temperature is from about 160° C. to about 190° C.
Aspect 30: The method of aspects 28 or 29, wherein the method further comprises transporting the second separation liquid having the fourth temperature to a separator tank.
Aspect 31: The method of aspect 30, wherein the method further comprises the steps of: e) providing a first product gas stream comprising a first wax product and a first lower hydrocarbon product, wherein the first gas product has a first temperature and the first wax product and first lower hydrocarbon product are in gas form; and f) separating at least a portion of the first wax product from the first product gas stream by lowering the first temperature of the first product gas stream by contacting the first product gas stream with the second separation liquid having the fourth temperature, thereby liquefying or solidifying at least a portion of the first wax product into the second separation, thereby producing a second product gas stream comprising at least a portion of the first lower hydrocarbon product.
Aspect 32: The method of aspect 31, wherein the first product gas stream comprising less than 5% of the first wax product.
Aspect 33: The method of aspects 31 or 32, wherein the second product gas stream comprising less than 0.5% of the first wax product.
Aspect 34: The method of any one of aspects 31-33, wherein the first product gas stream comprising from about 50% to about 99.5% of the first lower hydrocarbon product.
Aspect 35: The method of any one of aspects 31-34, wherein at least 50% of the first wax product is separated from the first product gas stream.
Aspect 36: The method of any one of aspects 31-35, wherein at least 80% of the first wax product is separated from the first product gas stream.
Aspect 37: The method of any one of aspects 31-36, wherein at least 90% of the first wax product is separated from the first product gas stream.
Aspect 38: The method of any one of aspects 31-37, wherein the first hydrocarbon product comprises C2-C5 hydrocarbons.
Aspect 39: The method of any one of aspects 19-38, wherein the first separation liquid comprises silicon oil, an ionic liquid, or a glycol, or a combination thereof.
Aspect 40: A system comprising: a) a separator tank comprising a first inlet, a second inlet, a first outlet, and a second outlet; b) a heat exchanger; c) a holding tank comprising a third inlet and a third outlet, wherein the separator tank is in fluid communication with the holding tank via a first connector and via a second connector, wherein the first connector is connected to the first outlet of the separator tank and to the third inlet of the holding tank, wherein the second connector is connected to the first inlet of the separator tank and to the third outlet of the holding tank, and wherein the first connector and the second connector are in communication with the heat exchanger.
Aspect 41: The system of aspect 40, wherein the system further comprises a Fisher-Tropsch reactor comprising a fourth inlet and a fourth outlet, wherein the separator tank is in fluid communication with the Fisher-Tropsch via a third connector, wherein the third connector is connected to the to the fourth outlet of the Fisher-Tropsch reactor and the second inlet of the separator tank.
Aspect 42: The system of aspect 40 or 41, wherein separator tank is configured to withstand pressure above 15 bar.
Aspect 43: The system of any one of aspect 40-42, wherein the holding tank is configured to hold at least 1,000 liters of separation fluid.
Aspect 44: The system of any one of aspect 40-43, wherein the separator tank is configured to hold at least 1,000 liters of separation fluid.
Aspect 45: The system of any one of aspect 40-44, wherein the second connector is in communication with a pump.
Aspect 46: The system of any one of aspect 40-45, wherein the separator tank comprises a fifth outlet.
Aspect 47: The system of any one of aspect 40-46, wherein the holding tank comprises a sixth outlet.
This application claims the benefit of U.S. Provisional Application No. 62/084,644, filed Nov. 26, 2014, which application is incorporated hereby by reference in its entirety.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/IB2015/058895 | 11/17/2015 | WO | 00 |
| Number | Date | Country | |
|---|---|---|---|
| 62084644 | Nov 2014 | US |
