WO2019016757A1

WO2019016757A1 - Apparatuses and methods related to the separation of wax products from products

Info

Publication number: WO2019016757A1
Application number: PCT/IB2018/055390
Authority: WO
Inventors: Shehzada Khurram; Talal Khaled AL-SHAMMARI; Khalid Karim; Thabet AL-QAHTANI; Abdullah Turki AL-JALOUD; Saud AL-KHUDEER
Original assignee: SABIC Global Technologies BV
Current assignee: SABIC Global Technologies BV
Priority date: 2017-07-21
Filing date: 2018-07-19
Publication date: 2019-01-24
Anticipated expiration: 2020-01-21

Abstract

Disclosed herein is an apparatus that includes a) an isothermal or adiabatic fixed bed reactor; b) a first condenser; and c) a second condenser, wherein the first condenser and the second condenser are in parallel fluid communication with the isothermal or adiabatic fixed bed reactor via a first connector.

Description

APPARATUSES AND METHODS RELATED TO THE SEPARATION OF WAX

PRODUCTS FROM PRODUCTS

CROSS-REFERENCE TO RELATED APPLICATIONS

[0001] This application claims priority to and the benefit of U.S. provisional application 62/535,503, filed on July 21, 2017, which is incorporated herein by reference in its entirety.

BACKGROUND

[0002] Syngas (mixtures of hydrogen (¾)) 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.

[0003] The product stream produced in a Fischer-Tropsch catalytic process comprises C2- C10 hydrocarbons and wax.

[0004] Accordingly, an apparatus and a method that separate wax from a product stream comprising hydrocarbons are disclosed herein.

SUMMARY OF THE INVENTION

[0005] Disclosed herein is an apparatus comprising: a) an isothermal or adiabatic fixed bed reactor; b) a first condenser; and c) a second condenser, wherein the first condenser and the second condenser are in parallel fluid communication with the isothermal or adiabatic fixed bed reactor via a first connector.

[0006] Disclosed herein is a method comprising the steps of: providing a first product gas stream comprising a wax product and a hydrocarbon product, wherein the wax product and the hydrocarbon product are in gas form; b) separating the wax product from the first product gas stream by lowering the temperature of the first product gas stream by passing the first product gas stream into a first condenser, thereby liquefying or solidifying a portion of the wax product, and producing a second product gas stream comprising at least a portion of the hydrocarbon product in gas form; c) collecting a predetermined amount of the wax product in the first condenser; d) discontinuing the step of passing the first product gas stream into the first condenser once the predetermined amount of the wax product is collected; and e) continuing to separate the wax product from the first product gas stream by lowering the temperature of the first product gas stream by passing the first product gas stream into a second condenser, thereby liquefying or solidifying a portion of the wax product, thereby producing a third product gas stream comprising at least a portion of the hydrocarbon product in gas form.

[0007] 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.

DESCRIPTION OF THE FIGURES

[0008] 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.

[0009] FIG. 1 shows an exemplary apparatus disclosed herein.

[0010] 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.

DETAILED DESCRIPTION

[0011] 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.

1. Definitions

[0012] 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:

[0013] 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.

[0014] 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.

[0015] 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. [0016] 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.

[0017] As used herein, the term space time yield ("STY") refers to the tons or kg of product that is produced per unit time per volume of catalyst.

[0018] As used herein, the term "wax" refers to a hydrocarbon having at least 1 lcarbon atoms, a CI 1+ hydrocarbon. For example, the wax can be a CI 1-C120 hydrocarbon, such as for example a CI 1-C40 hydrocarbon, a C20-C40 hydrocarbon, a C20-C60 hydrocarbon, a C20-C80 hydrocarbon, or a C20-C110 hydrocarbon. The wax is produced as a by-product in a Fischer-Tropsch process, which aims to produce C2-C10 hydrocarbons from syngas.

2. Apparatus

[0019] The Fischer-Tropsch catalytic process for producing hydrocarbons from syngas is known in the art.

[0020] The production of wax, CO₂, and CH₄ is unwanted in Fischer-Tropsch processes, which targets the production of hydrocarbons (C2-C10 hydrocarbons, for example, C2-C6). Waxes produced from Fischer-Tropsch processes are typically paraffin waxes, that is, a mixture of hydrocarbon molecules, wherein each molecule contains from 11 to 120 carbon atoms. It is desired to separate the wax from the C2-C10 hydrocarbons in the product stream so that the C2-C10 hydrocarbons can be further processed in downstream processes. The apparatus and method disclosed herein provide means for separating wax from other hydrocarbons, such as, for example, C2-C10 hydrocarbons.

[0021] An exemplary carbon distribution of a wax produced in a Fischer-Tropsch process is shown in Table 1.

TABLE 1

C19 4.52%

C20 5.54%

C21 6.67%

C22 7.29%

C23 7.95%

C24 8.24%

C25 8.06%

C26 7.38%

C27 6.62%

C28 5.80%

C29 4.77%

C30 3.96%

C31 2.98%

C32 2.33%

C33 1.94%

C34 1.27%

C35 0.56%

C36 0.30%

C37 0.16%

C38 0.08%

[0022] 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 first product gas stream comprising a wax product and a hydrocarbon product. The amount of a wax product in the first product gas stream is less than 5 wt %. In one aspect, the amount of a wax product in the hydrocarbon products is less than 4 wt %, 3 wt %, 2 wt %, or 1 wt %.

[0023] In one aspect, the first product gas stream can comprise a wax product, a hydrocarbon product, water, and at least one alcohol.

[0024] It is desired for a Fischer-Tropsch process, including downstream processing of products, to run continuously. Starting and stopping an industrial Fischer-Tropsch process is both costly and time consuming. In one aspect, the Fischer-Tropsch process produces a first product gas stream comprising a wax product and a hydrocarbon product. It is desired to separate the wax product from hydrocarbon product. As such, it is desired that the separation of the wax product from the hydrocarbon product can be done continuously without having to stop the Fischer-Tropsch process to remove wax or clean equipment, such as remove wax from or clean a condenser, that can be used to separate the wax product from hydrocarbon product. For example, a condenser can only hold a certain amount of wax before a portion of the wax has to be removed to make more space for additional wax to be collected. The apparatus disclosed herein can be operated such that the wax product can be continuously separated from a first product gas stream comprising a wax product and a hydrocarbon product.

[0025] Disclosed herein is an apparatus comprising: a) an isothermal or adiabatic fixed bed reactor; b) a first condenser; and c) a second condenser, wherein the first condenser and the second condenser are in parallel fluid communication with the isothermal or adiabatic fixed bed reactor via a first connector.

[0026] In one aspect, the first connector comprises a first line that is in fluid communication with the first condenser, and wherein the first line comprises a valve that configured to regulate the flow of a first product gas stream comprising a wax product and a hydrocarbon product from the isothermal or adiabatic fixed bed reactor to the first condenser.

[0027] In one aspect, the first connector comprises a second line that is in fluid

communication with the second condenser, and wherein the second line comprises a valve that configured to regulate the flow of a first product gas stream comprising a wax product and a hydrocarbon product from the isothermal or adiabatic fixed bed reactor to the second condenser.

[0028] Both the wax product and the hydrocarbon product are in gas form in the first product gas. The wax product has a lower boiling point than the hydrocarbon product. The first condenser and the second condenser lower the temperature of the first product gas such that the temperature is below the boiling point of the wax product but above the boiling point of the hydrocarbon products. As such, the wax product liquefies or solidifies in the condenser while the hydrocarbon product remains in gas form, thereby separating the wax product from the hydrocarbon product in the first product gas stream. The hydrocarbon product remains in gas form and exits the condenser, such as the first condenser or second condenser, for further processing.

[0029] In one aspect, the temperature of the first product gas stream from about 230 °C to about 250 °C. In another aspect, the condenser, such as the first condenser or second condenser, lowers the temperature of the first product gas stream such that the temperature is from about 160 °C to about 190 °C.

[0030] At the onset of operation, the valve in the first line is open to allow the first product gas stream to flow from the isothermal or adiabatic fixed bed reactor to the first condenser, while the valve in the second line is closed to prevent the first product stream from reaching the second condenser. Once a predetermined amount of the first wax product is collected in the first condenser the valve in the first line is closed, and the valve in the second line is opened to redirect the flow of the first product gas stream from the first condenser to the second condenser. The wax that was collected in the first condenser can be removed while the second condenser is used to continue the process of separating the first wax product from the hydrocarbon product in the first product gas stream. Similarly, when a predetermined of the first wax product is collected in the second condenser the valve in the second line is closed and the valve in the first line is reopened to redirect the flow of the first product gas stream from the second condenser to the first condenser. This is done after a portion of the wax product in the first condenser that was first collected has been removed to allow more wax product to be collected in the first condenser. The wax product in the second condenser can be removed while the first condenser again is used to continue the process of separating the first wax product from the hydrocarbon product in the first product gas stream. The use of the first condenser and the second condenser can be alternated in this way such that the apparatus can be used in operation continuously.

[0031] In one aspect, the first condenser is configured to withstand at least a pressure of above about 12 bar. For example, the first condenser can be configured to withstand at least a pressure from about 12 bar to about 20 bar.

[0032] In one aspect, the second condenser is configured to withstand at least a pressure of above about 12 bar. For example, the first condenser can be configured to withstand at least a pressure from about 12 bar to about 20 bar.

[0033] In one aspect, the isothermal or adiabatic fixed bed reactor, first condenser, and second condenser is configured to support a Fischer-Tropsch system on an industrial scale.

[0034] For example, the isothermal or adiabatic fixed bed reactor can be configured to hold at least a volume about 1,000 liter. In another example, the isothermal or adiabatic fixed bed reactor can be configured to have a volume from about 1,000 liters to about 20,000 liters.

[0035] In one aspect, the first condenser is configured to support a Fischer-Tropsch system on an industrial scale. For example, the first condenser is configured to collect a volume of the wax product on an industrial scale. For example, the first condenser can be configured to collect at least about 10 liters of the wax produce. In another example, the first condenser can be configured to have a volume from about 10 liters to about 20,000 liter.

[0036] In one aspect, the second condenser is configured to support a Fischer-Tropsch system on an industrial scale. For example, the second condenser is configured to collect a volume of the wax product on an industrial scale. For example, the second condenser can be configured to collect at least about 10 liters of the wax produce. In another example, the second condenser can be configured to have a volume from about 10 liters to about 20,000 liter.

[0037] Optionally, in various aspects, the disclosed apparatus can be operated or configured on an industrial scale. In one aspect, the apparatus, and methods disclosed herein can be configured to produce a first product gas stream comprising a wax product and a hydrocarbon product on an industrial scale.

[0038] 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 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 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.

[0039] In one aspect, the disclosed apparatus and method can have a STY of at least 0.5/kg/hr of catalyst for the reactors disclosed herein. For example, the disclosed apparatus and method can have a STY of at least 0.7/kg/hr of catalyst for the isothermal or adiabatic fixed bed reactor disclosed herein. In another example, the disclosed apparatus and method can have a STY from 0.5 to 1/kg/hr of catalyst for the isothermal or adiabatic fixed bed reactor disclosed herein.

[0040] In additional aspects, the components of the disclosed apparatus can be shaped and sized to permit production of a first product gas stream comprising a wax product and a hydrocarbon product on an industrial scale.

[0041] Now referring to FIG. 1, which shows a non-limiting exemplary aspect of the apparatus disclosed herein. FIG. 1 shows an apparatus (100). The apparatus (100) has an isothermal or adiabatic fixed bed reactor (102). The apparatus (100) also has a first condenser (104) and a second condenser (106). The first condenser (104) and the second condenser (106) are in parallel fluid communication with the isothermal or adiabatic fixed bed reactor (102) via a first connector (108). The first connector (108) comprises a first line (110) and a second line (112). The first line (110) has a valve (116) that is configured to regulate the flow of a first product gas stream comprising a wax product and a hydrocarbon product from the isothermal or adiabatic fixed bed reactor (102) to the first condenser (104). The second line (112) has a valve (118) that is configured to regulate the flow of a first product gas stream comprising a wax product and a hydrocarbon product from the isothermal or adiabatic fixed bed reactor (102) to the second condenser (106). A second connector (114) can be in fluid communication with the isothermal or adiabatic fixed bed reactor (102) and is configured to transport syngas to the isothermal or adiabatic fixed bed reactor (102). The first condenser (104) and the second condenser (106) are configured to remove at least a portion of the wax product in the first product gas stream to respectively produce a second product gas stream (120) comprising the hydrocarbon product and a second product gas stream (122) comprising the hydrocarbon product.

3. Methods

[0042] The apparatus disclosed herein can be used to perform the method disclosed herein.

[0043] Disclosed herein is a method comprising the steps of: providing a first product gas stream comprising a wax product and a hydrocarbon product, wherein the wax product and the hydrocarbon product are in gas form; b) separating the wax product from the first product gas stream by lowering the temperature of the first product gas stream by passing the first product gas stream into a first condenser, thereby liquefying or solidifying a portion of the wax product, and producing a second product gas stream comprising at least a portion of the hydrocarbon product in gas form; c) collecting a predetermined amount of the wax product in the first condenser; d) discontinuing the step of passing the first product gas stream into the first condenser once the predetermined amount of the wax product is collected; and e) continuing to separate the wax product from the first product gas stream by lowering the temperature of the first product gas stream by passing the first product gas stream into a second condenser, thereby liquefying or solidifying a portion of the wax product, thereby producing a third product gas stream comprising at least a portion of the hydrocarbon product in gas form.

[0044] In one aspect, the method further comprises the step of: f) removing at least a portion of the wax product from the first condenser after the predetermined amount of the wax product has been collected. In another aspect, the method further comprises the steps of: g) collecting a predetermined amount of the wax product in the second condenser; h) discontinuing the step of passing the first product gas stream into the second condenser once the predetermined amount of the wax product is collected in the second condenser; and i) continuing to separate the wax product from the product gas stream by lowering the temperature of the first product gas stream by passing the first product gas stream into the first condenser, thereby liquefying or solidifying a portion of the wax product, thereby producing the second product gas stream comprising at least a portion of the hydrocarbon product in gas form.

[0045] As described above, the method disclosed herein allows for a Fischer-Tropsch process to be performed continuously without the need for discontinuing the process to remove collected wax product from a condenser. Accordingly, in one aspect, method steps a)-i) can be repeated at least once. For example, method steps a)-i) can be repeated at least twice, thrice, or four times. In another example, method steps a)-i) can be repeated from 1 to 100 times, such as from 1 to 20 times. In another example, method steps a)-i) can be repeated over a predetermined time such as for at least 1 day, 3 days, 1 week, or 4 weeks. For example, the predetermined time can be from 1 day to 4 weeks.

[0046] In one aspect, the first product gas stream comprising a wax product and hydrocarbon product is produced in a Fischer-Tropsch process. The Fischer-Tropsch process produces a first product gas stream comprising less than 5 wt % of the wax product. For example, the Fischer-Tropsch process can produce a first product gas stream comprising less than 4 wt %, 3 wt %, 2 wt %, or 1 wt % of the wax product. In another example, the Fischer-Tropsch process can produce a first product gas stream comprising from about 1 wt % to about 5 wt % of the wax product.

[0047] In one aspect, the first product gas stream has a temperature of from about 230 °C to about 250 °C. For example, the first product gas stream can have a temperature of from about 235 °C to about 245 °C.

[0048] The condenser, such as the first condenser or second condenser, lowers the temperature of the first product gas stream such that the temperature is from about 160 °C to about 190 °C. Under operating pressure, the a wax product liquefies or solidifies in the condenser at this temperature while the hydrocarbon product remains in gas form, thereby separating the wax product from the hydrocarbon product in the first product gas stream, thereby producing the second product gas stream comprising a portion of the hydrocarbon product in gas form.

[0049] In one aspect, the second product gas stream comprising a portion of the hydrocarbon product in gas form has a temperature of about 160 °C to about 190 °C. For example, the second product gas stream comprising a portion of the hydrocarbon product in gas form has a temperature of about 165 °C to about 185 °C, such as, from about 170 °C to about 180 °C.

[0050] The second product gas stream can be substantially free of the wax product. In one aspect, the second product gas stream can comprise less than about 0.1 wt % of the wax product. For example, the second product gas stream can comprise less than about 0.05 wt % of the wax product. In another example, the second product gas stream can comprise from about 0.001 wt % to about 0.1 wt %, such as 0.01 wt % to about 0.05 wt % of the wax product.

[0051] In one aspect, the third product gas stream comprising a portion of the hydrocarbon product in gas form has a temperature of about 160 °C to about 190 °C. For example, the third product gas stream comprising a portion of the hydrocarbon product in gas form has a temperature of about 165 °C to about 185 °C, such as, from about 170 °C to about 180 °C.

[0052] The third product gas stream can be substantially free of the wax product. In one aspect, the third product gas stream can comprise less than about 0.1 wt % of the wax product. For example, the third product gas stream can comprise less than about 0.05 wt % of the wax product. In another example, the third product gas stream can comprise from about 0.001 wt % to about 0.1 wt %, such as 0.01 wt % to about 0.05 wt % of the wax product.

[0053] In one aspect, at least 50% of the wax product is separated from the first product gas stream. For example, at least 70% of the wax product is separated from the first product gas stream. In another example, at least 80% of the wax product can be separated from the first product gas stream. In yet another example, at least 85% of the wax product can be separated from the first product gas stream. In another example, at least 90% of the wax product can be separated from the first product gas stream. In another example, at least 95% of the wax product can be separated from the first product gas stream. In another example, at least 97% of the wax product can be separated from the first product gas stream. In another example, at least 99% of the wax product can be separated from the first product gas stream.

[0054] In one aspect, the first product gas stream comprises from about 50% to about 99% of the hydrocarbon product. For example, the first product gas stream can comprise from about 50% to about 90% of the hydrocarbon product. In another example, the first product gas stream can comprise from about 60% to about 80% of the hydrocarbon product.

[0055] In one aspect, the first hydrocarbon product comprises C2-C6 hydrocarbons.

[0056] 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.

[0057] In one aspect, the 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.

[0058] The method disclosed herein comprises the step of collecting a predetermined amount of the wax product in the first condenser. In one aspect, the predetermined amount of the wax product can be at least about 50 % of the holding capacity of the first condenser. For example, the predetermined amount of the wax product can be at least about 60 %, 70 %, 80 %, or 90 % of the holding capacity of the first condenser. In another example, the predetermined amount of the wax product can be from about 60 % to about 90 % of the holding capacity of the first condenser.

[0059] The method disclosed herein can comprise the step of collecting a predetermined amount of the wax product in the second condenser. In one aspect, the predetermined amount of the wax product can be at least about 50 % of the holding capacity of the second condenser. For example, the predetermined amount of the wax product can be at least about 60 %, 70 %, 80 %, or 90 % of the holding capacity of the second condenser. In another example, the predetermined amount of the wax product can be from about 60 % to about 90 % of the holding capacity of the second condenser.

4. Aspects

[0060] 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.

[0061] Aspect 1 : A method comprising the steps of: a) providing a first product gas stream comprising a wax product and a hydrocarbon product, wherein the wax product and the hydrocarbon product are in gas form; b) separating the wax product from the product gas stream by lowering the temperature of the first product gas stream by passing the first product gas stream into a first condenser, thereby liquefying or solidifying a portion of the wax product, and producing a second product gas stream comprising at least a portion of the hydrocarbon product in gas form; c) collecting a predetermined amount of the wax product in the first condenser; d) discontinuing the step of passing the first product gas stream into the first condenser once the predetermined amount of the wax product is collected; and e) continuing to separate the wax product from the first product gas stream by lowering the temperature of the first product gas stream by passing the product gas stream into a second condenser, thereby liquefying or solidifying a portion of the wax product, thereby producing a third product gas stream comprising at least a portion of the hydrocarbon product in gas form.

[0062] Aspect 2: The method of aspect 1, wherein first product gas comprising the wax product and the hydrocarbon product is produced in a Fischer-Tropsch process.

[0063] Aspect 3 : The method of aspects 1 or 2, wherein the hydrocarbon product comprises C2-C6 hydrocarbons.

[0064] Aspect 4: The method of any one of aspects 1-3, wherein the first product gas stream in step a) has a temperature of from about 230 °C to about 250 °C.

[0065] Aspect 5 : The method of aspect 4, wherein the second product gas stream has a temperature of from about 160 °C to about 190 °C.

[0066] Aspect 6: The method of any one of aspects 1-5, wherein the first product gas stream before lowering the temperature in step e) has a temperature of from about 230 °C to about 250 °C.

[0067] Aspect 7: The method of aspect 6, wherein the third product gas stream has a temperature of from about 160 °C to about 190 °C.

[0068] Aspect 8: The method of any one of aspects 1-7, wherein the method is continuous. [0069] Aspect 9: The method of any one of aspects 1-8, wherein the second product gas stream comprises at least 95 wt % of the hydrocarbon product.

[0070] Aspect 10: The method of any one of aspects 1-9, wherein the third product gas stream comprises at least 95 wt % of the hydrocarbon product.

[0071] Aspect 11 : The method of any one of aspects 1-10, wherein the second product gas stream comprises less than 0.1 wt % of the wax product.

[0072] Aspect 12: The method of any one of aspects 1-11, wherein the third product gas stream comprises less than 0.1 wt % of the wax product.

[0073] Aspect 13: The method of any one of aspects 1-12, wherein the method further comprises the step of: f) removing at least a portion of the wax product from the first condenser after the predetermined amount of the wax product has been collected.

[0074] Aspect 14: The method of aspect 13, wherein the method further comprises the steps of: g) collecting a predetermined amount of the wax product in the second condenser; h) discontinuing the step of passing the first product gas stream into the second condenser once the predetermined amount of the wax product is collected in the second condenser; and i) continuing to separate the wax product from the first product gas stream by lowering the temperature of the first product gas stream by passing the product gas stream into the first condenser, thereby liquefying or solidifying a portion of the wax product, thereby producing the second product gas stream comprising at least a portion of the hydrocarbon product in gas form.

[0075] Aspect 15: The method of any one of aspects 1-14, wherein steps a)-i) are repeated at least once.

[0076] Aspect 16: The method of any one of aspects 1-15, wherein the method is performed using an apparatus comprising: a) an isothermal or adiabatic fixed bed reactor; b) a first condenser; and c) a second condenser, wherein the first condenser and the second condenser are in parallel fluid communication with the isothermal or adiabatic fixed bed reactor via a first connector.

[0077] Aspect 17: An apparatus comprising: a) an isothermal or adiabatic fixed bed reactor; b) a first condenser; and c) a second condenser, wherein the first condenser and the second condenser are in parallel fluid communication with the isothermal or adiabatic fixed bed reactor via a first connector.

[0078] Aspect 18: The apparatus of aspect 17, wherein the first connector comprises a first line that is in fluid communication with the first condenser, and wherein the first line comprises a valve that configured to regulate the flow of a first product gas stream comprising a wax product and a hydrocarbon product from the isothermal or adiabatic fixed bed reactor to the first condenser.

[0079] Aspect 19: The apparatus of aspects 17 or 18, wherein the first connector comprises a second line that is in fluid communication with the second condenser, and wherein the second line comprises a valve that configured to regulate the flow of a first product gas stream comprising a wax product and a hydrocarbon product from the isothermal or adiabatic fixed bed reactor to the second condenser.

[0080] Aspect 20: The apparatus of any one of aspects 17-19, wherein the apparatus in an industrial sized apparatus.

[0081] Various modifications and variations can be made to the compounds, composites, kits, articles, devices, compositions, and methods described herein. Other aspects of the compounds, composites, kits, articles, devices, compositions, and methods described herein will be apparent from consideration of the specification and practice of the compounds, composites, kits, articles, devices, compositions, and methods disclosed herein. It is intended that the specification and examples be considered as exemplary.

Claims

CLAIMS claimed is:

1. A method comprising the steps of: a) providing a first product gas stream comprising a wax product and a

hydrocarbon product, wherein the wax product and the hydrocarbon product are in gas form;

b) separating the wax product from the product gas stream by lowering the

temperature of the first product gas stream by passing the first product gas stream into a first condenser, thereby liquefying or solidifying a portion of the wax product, and producing a second product gas stream comprising at least a portion of the hydrocarbon product in gas form;

c) collecting a predetermined amount of the wax product in the first condenser; d) discontinuing the step of passing the first product gas stream into the first condenser once the predetermined amount of the wax product is collected; and e) continuing to separate the wax product from the first product gas stream by lowering the temperature of the first product gas stream by passing the product gas stream into a second condenser, thereby liquefying or solidifying a portion of the wax product, thereby producing a third product gas stream comprising at least a portion of the hydrocarbon product in gas form.

2. The method of claim 1, wherein first product gas comprising the wax product and the hydrocarbon product is produced in a Fischer-Tropsch process.

3. The method of claims 1 or 2, wherein the hydrocarbon product comprises C2- C6 hydrocarbons.

4. The method of any one of claims 1-3, wherein the first product gas stream in step a) has a temperature of from about 230 °C to about 250 °C.

5. The method of claim 4, wherein the second product gas stream has a

temperature of from about 160 °C to about 190 °C.

6. The method of any one of claims 1-5, wherein the first product gas stream before lowering the temperature in step e) has a temperature of from about 230 °C to about 250 °C.

7. The method of claim 6, wherein the third product gas stream has a temperature of from about 160 °C to about 190 °C.

8. The method of any one of claims 1-7, wherein the method is continuous.

9. The method of any one of claims 1-8, wherein the second product gas stream comprises at least 95 wt % of the hydrocarbon product.

10. The method of any one of claims 1-9, wherein the third product gas stream comprises at least 95 wt % of the hydrocarbon product.

11. The method of any one of claims 1-10, wherein the second product gas stream comprises less than 0.1 wt % of the wax product.

12. The method of any one of claims 1-11, wherein the third product gas stream comprises less than 0.1 wt % of the wax product.

13. The method of any one of claims 1-12, wherein the method further comprises the step of: f) removing at least a portion of the wax product from the first condenser after the predetermined amount of the wax product has been collected.

14. The method of claim 13, wherein the method further comprises the steps of: g) collecting a predetermined amount of the wax product in the second condenser; h) discontinuing the step of passing the first product gas stream into the second condenser once the predetermined amount of the wax product is collected in the second condenser; and i) continuing to separate the wax product from the first product gas stream by lowering the temperature of the first product gas stream by passing the product gas stream into the first condenser, thereby liquefying or solidifying a portion of the wax product, thereby producing the second product gas stream comprising at least a portion of the hydrocarbon product in gas form.

15. The method of any one of claims 1-14, wherein steps a)-i) are repeated at least once.

16. The method of any one of claims 1-15, wherein the method is performed using an apparatus comprising: a) an isothermal or adiabatic fixed bed reactor;

b) a first condenser; and

c) a second condenser, wherein the first condenser and the second condenser are in parallel fluid communication with the isothermal or adiabatic fixed bed reactor via a first connector.

17. An apparatus comprising: a) an isothermal or adiabatic fixed bed reactor;

b) a first condenser; and

c) a second condenser,

wherein the first condenser and the second condenser are in parallel fluid communication with the isothermal or adiabatic fixed bed reactor via a first connector.

18. The apparatus of claim 17, wherein the first connector comprises a first line that is in fluid communication with the first condenser, and wherein the first line comprises a valve that configured to regulate the flow of a first product gas stream comprising a wax product and a hydrocarbon product from the isothermal or adiabatic fixed bed reactor to the first condenser.

19. The apparatus of claims 17 or 18, wherein the first connector comprises a second line that is in fluid communication with the second condenser, and wherein the second line comprises a valve that configured to regulate the flow of a first product gas stream comprising a wax product and a hydrocarbon product from the isothermal or adiabatic fixed bed reactor to the second condenser.

The apparatus of any one of claims 17-19, wherein the apparatus in an industrial sized apparatus.