The systems and methods for liquid hydrocarbon production from natural gas

Abstract

Exemplary systems and methods convert stranded natural gas (SNG) to liquid fuels. Broadly, exemplary systems and methods include a reforming stage, a heat integration stage, and a liquid fuel generation stage.

Description

Attorney Docket No.029784-0011-WO01 THE SYSTEMS AND METHODS FOR LIQUID HYDROCARBON PRODUCTION FROM NATURAL GAS CROSS-REFERENCE TO RELATED APPLICATIONS

[0001] This application claims priority to U.S. Provisional Patent Application No.63 / 653,634, filed on May 30, 2024, and U.S. Provisional Patent Application No.63 / 658,723, filed on June 11, 2024, the entire contents of which are incorporated herein by reference. STATEMENT OF GOVERNMENT SUPPORT

[0002] This invention was made with government support under 2029282, awarded by the National Science Foundation. The government has certain rights in the invention. TECHNICAL FIELD

[0003] The present disclosure generally relates to the production of liquid hydrocarbons from natural gas using a reactor system. Exemplary methods and operating strategies may be particularly suited for using stranded natural gas. INTRODUCTION

[0004] The increasing global awareness towards energy-saving policies has instilled the need for successful technologies for the utilization of stranded natural gas (SNG) reserves. SNG refers to gas reservoirs that are geographically isolated or economically unviable to transport via conventional pipeline infrastructure to markets where demand exists. Typically, oil wells producing between 1,600 and 3,200 barrels of oil equivalents per day often produce about 63,000 cubic feet per hour of natural gas. Such reserves, with a size smaller than 0.5 trillion cubic feet or located further than 100 km from the product market, are typically flared without being utilized due to their lack of economic viability, which results in increased carbon dioxide (CO2) emissions. SUMMARY

[0005] In some aspects, the techniques described herein relate to a method for operating a reactor system including a reformer reactor, a heat exchange unit, and a Fischer-Tropsch reactor,Attorney Docket No.029784-0011-WO01 the method including: heating the reformer reactor using air and fuel; providing a reformer reactor input stream to the reformer reactor, the reformer reactor input stream including natural gas (CH4), carbon dioxide (CO2), and steam (H2O); collecting a reformer reactor output stream generated in the reformer reactor from a reformer reactor outlet, the reformer reactor output stream including carbon monoxide (CO) and hydrogen (H2); providing the reformer reactor output stream to a first input of the heat exchange unit, collecting a first heat exchange output stream from a heat exchange unit outlet, the first heat exchange output stream including carbon monoxide (CO) and hydrogen (H2); and the first heat exchange output stream having a lower temperature than the reformer reactor output stream; providing the first heat exchange output stream to the Fischer-Tropsch reactor; collecting a Fischer-Tropsch reactor output stream from the Fischer-Tropsch reactor, the Fischer-Tropsch reactor output stream including hydrocarbon products.

[0006] In some aspects, the techniques described herein relate to a reactor system, including: a reformer reactor including: a reformer reactor inlet in fluid communication with a reformer reactor input stream source and configured to receive the reformer reactor input stream, the reformer reactor input stream including natural gas (CH4), carbon dioxide (CO2), and steam (H2O); a reformer reactor outlet configured to provide a reformer reactor output stream, the reformer reactor output stream including carbon monoxide (CO) and hydrogen (H2); a heat exchange unit including a plurality of inlets and a plurality of outlets, the heat exchange unit configured to: increase a temperature of a plurality of input streams with the reformer reactor output stream, the plurality of input streams including a steam stream, a carbon dioxide (CO2) stream, and a natural gas (CH4) stream; decrease a temperature of the reformer reactor output stream; collect water condensed from the reformer reactor output stream; wherein one of the plurality of outlets includes a syngas outlet; a Fischer-Tropsch reactor including: a catalyst bed; a Fischer-Tropsch reactor inlet in fluid communication with the syngas outlet of the heat exchange unit and configured to distribute syngas over the catalyst bed and generate hydrocarbon products; a Fischer-Tropsch reactor outlet configured to provide the hydrocarbon products.Attorney Docket No.029784-0011-WO01 BRIEF DESCRIPTION OF THE DRAWINGS

[0007] FIG.1 is a schematic diagram of an exemplary reactor system.

[0008] FIG.2 is a schematic process flow diagram of another exemplary reactor system.

[0009] FIG.3 is a schematic process flow diagram of another exemplary reactor system.

[0010] FIG.4 is a schematic process flow diagram of another exemplary reactor system.

[0011] FIG.5 shows an exemplary, vertically arranged reactor system.

[0012] FIG.6 shows another exemplary, vertically arranged reactor system and other process components.

[0013] FIG.7 schematically illustrates an exemplary method of operating a reactor system.

[0014] FIG. 8A schematically illustrates a first portion of a system used for computational simulations of Case-0. FIG. 8B schematically illustrates a second portion of the system used for computational simulations of Case-0.

[0015] FIG. 9A schematically illustrates a first portion of a system used for computational simulations of Case-1. FIG. 9B schematically illustrates a second portion of the system used for computational simulations of Case-1. FIG. 9C schematically illustrates a third portion of the system used for computational simulations of Case-1.

[0016] FIG. 10A schematically illustrates a first portion of a system used for computational simulations of Case-2. FIG. 10B schematically illustrates a second portion of the system used for computational simulations of Case-2.

[0017] FIG. 11A schematically illustrates a first portion of a system used for computational simulations of Case-3. FIG. 11B schematically illustrates a second portion of the system used for computational simulations of Case-3. DETAILED DESCRIPTION

[0018] The present disclosure relates to systems and methods for converting stranded natural gas (SNG) to liquid fuels. Broadly, exemplary systems and methods include a reforming stage, a heat integration stage, and a liquid fuel generation stage.

[0019] In some instances, the mixed reforming stage converts stranded natural gas containing a mix of alkanes to high-purity syngas. Reforming employs a mixed metal oxide catalyst toAttorney Docket No.029784-0011-WO01 convert SNG to syngas, enabling a co-utilization of carbon dioxide (CO2) and steam, asrepresented by Equation 1 below.+ + + (1)

[0020] The reforming reaction is endothermic in nature, and the required heat can be supplied by flaring a supplementary amount of SNG or electric heating. The resulting syngas stream exits the reforming stage at a high temperature. This heat can be recovered in the second stage of this process, which is a heat integration network. The heat from the flue gas can be used to preheat other process streams that include but are not limited to air, SNG, and CO2, along with the generation of superheated steam. The second stage can be subdivided into a series of multi- tubular heat exchangers around which the process fluids are circulated to facilitate heat transfer. Additionally, the flue gas produced by flaring supplementary SNG may provide heat for the reformer and by flaring out any downstream light-ends can also be utilized for pre-heating the process streams.

[0021] The third stage includes a Fischer-Tropsch (F.T.) section that can be a multi-tubular catalytic bed. The high-pressure syngas can be brought to the operating temperature of F.T. by utilizing the heat transfer assisted by the second stage. The pressurized high-purity syngas is converted into liquid fuels in the third stage of the modular reactor. The reaction taking place inthe F.T. section is represented by Equation 2.+(2)I. Definitions

[0022] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In case of conflict, the present document, including definitions, will control. Methods and materials are described below, although methods and materials similar or equivalent to those described herein can be used in practice or testing of the present disclosure. All publications, patent applications, patents and other references mentioned herein are incorporated by reference in their entirety. The materials, methods, and examples disclosed herein are illustrative only and not intended to be limiting.

[0023] The terms “comprise(s),” “include(s),” “having,” “has,” “can,” “contain(s),” and variants thereof, as used herein, are intended to be open-ended transitional phrases, terms, or words that do not preclude the possibility of additional acts or structures. The singular forms “a,” “an”Attorney Docket No.029784-0011-WO01 and “the” include plural references unless the context clearly dictates otherwise. The present disclosure also contemplates other embodiments “comprising,” “consisting of” and “consisting essentially of,” the embodiments or elements presented herein, whether explicitly set forth or not.

[0024] For the recitation of numeric ranges herein, each intervening number therebetween with the same degree of precision is contemplated. For example, for the range of 6-9, the numbers 7 and 8 are contemplated in addition to 6 and 9, and for the range 6.0-7.0, the numbers 6.0, 6.1, 6.2, 6.3, 6.4, 6.5, 6.6, 6.7, 6.8, 6.9, and 7.0 are contemplated. For another example, when a pressure range is described as being between ambient pressure and another pressure, a pressure that is ambient pressure is expressly contemplated.

[0025] Definitions of specific functional groups and chemical terms are described in more detail below. For purposes of this disclosure, the chemical elements are identified in accordance with the Periodic Table of the Elements, CAS version, Handbook of Chemistry and Physics, 75thEd., inside cover, and specific functional groups are generally defined as described therein. Additionally, general principles of organic chemistry, as well as specific functional moieties and reactivity, are described in Organic Chemistry, Thomas Sorrell, University Science Books, Sausalito, 1999; Smith and March March's Advanced Organic Chemistry, 5thEdition, John Wiley & Sons, Inc., New York, 2001; Larock, Comprehensive Organic Transformations, VCH Publishers, Inc., New York, 1989; Carruthers, Some Modern Methods of Organic Synthesis, 3rdEdition, Cambridge University Press, Cambridge, 1987; the entire contents of each of which are incorporated herein by reference. II. Exemplary Materials

[0026] Exemplary systems, methods, and techniques disclosed and contemplated herein may use and generate various materials. Exemplary materials may include input air, fuel, reformer reactor input streams, reformer reactor output streams, Fischer-Tropsch reactor input streams, and Fischer-Tropsch reactor output streams. Various aspects of each are described below.

[0027] Exemplary air comprises oxygen (O2). In some instances, exemplary air may be heated above ambient temperature. Exemplary air may further comprise argon (Ar) and / or nitrogen (N2).

[0028] Exemplary reformer reactor input streams may comprise natural gas (CH4), carbon dioxide (CO2), and steam (H2O). Typically, the natural gas (CH4) is stranded natural gas. The term “stranded natural gas” refers to natural gas from gas reservoirs that are geographically isolated orAttorney Docket No.029784-0011-WO01 economically unviable to transport via conventional pipeline infrastructure to markets where demand exists.

[0029] In some implementations, the reformer reactor input streams are preheated prior to entering the reformer reactor. In various instances, preheated carbon dioxide (CO2) may be at a temperature between 450 °C and 650 °C. In various instances, preheated steam (H2O) may be at a temperature between 450 °C and 650 °C. In various instances, preheated stranded natural gas may be at a temperature between 400 °C and 600 °C. Exemplary reformer reactor input streams may further comprise light hydrocarbon material, which is described below.

[0030] In various instances, preheated carbon dioxide (CO2) may be at a temperature between 450 °C and 650 °C. In various instances, preheated carbon dioxide (CO2) may be at a temperature between 450 °C and 650 °C; 500 °C and 650 °C; 550 °C and 650 °C; 600 °C and 650 °C; 450 °C and 600 °C; 450 °C and 550 °C; or 450 °C and 500 °C. In various instances, preheated carbon dioxide (CO2) may be no less than 450 °C; no less than 500 °C; no less than 550 °C; no less than 600 °C; or no less than 650 °C. In various instances, preheated carbon dioxide (CO2) may be no greater than 650 °C; no greater than 600 °C; no greater than 550 °C; no greater than 500 °C; or no greater than 450 °C.

[0031] In various instances, preheated steam (H2O) may be at a temperature between 450 °C and 650 °C. In various instances, preheated steam (H2O) may be at a temperature between 450 °C and 650 °C; 500 °C and 650 °C; 550 °C and 650 °C; 600 °C and 650 °C; 450 °C and 600 °C; 450 °C and 550 °C; or 450 °C and 500 °C. In various instances, preheated steam (H2O) may be no less than 450 °C; no less than 500 °C; no less than 550 °C; no less than 600 °C; or no less than 650 °C. In various instances, preheated steam (H2O) may be no greater than 650 °C; no greater than 600 °C; no greater than 550 °C; no greater than 500 °C; or no greater than 450 °C.

[0032] In various instances, preheated stranded natural gas may be at a temperature between 400 °C and 600 °C. In various instances, preheated stranded natural gas may be at a temperature between 400 °C and 600 °C; 450 °C and 600 °C; 500 °C and 600 °C; 550 °C and 600 °C; 400 °C and 550 °C; 400 °C and 500 °C; or 400 °C and 450 °C. In various instances, preheated stranded natural gas may be no less than 400 °C; no less than 450 °C; no less than 500 °C; no less than 550 °C; or no less than 600 °C. In various instances, preheated stranded natural gas may be no greater than 600 °C; no greater than 550 °C; no greater than 500 °C; no greater than 450 °C; or no greaterAttorney Docket No.029784-0011-WO01 than 400 °C.

[0033] Exemplary reformer reactor output streams may comprise carbon monoxide (CO) and hydrogen (H2). Exemplary reformer reactor output streams may further comprise steam (H2O).

[0034] Exemplary reformer output streams may comprise a hydrogen (H2) / carbon monoxide (CO) ratio between 1.7 and 2.2.

[0035] In various instances, exemplary reformer output streams may comprise a hydrogen (H2) / carbon monoxide (CO) ratio between 1.7 and 2.2. In various instances, exemplary reformer output streams may comprise a hydrogen (H2) / carbon monoxide (CO) ratio between 1.7 and 2.2; 1.8 and 2.2; 1.9 and 2.2; 2.0 and 2.2; 2.1 and 2.2; 1.7 and 2.1; 1.7 and 2.0; 1.7 and 1.9; or 1.7 and 1.8. In various instances, exemplary reformer output streams may comprise a hydrogen (H2) / carbon monoxide (CO) ratio may be no less than 1,7; no less than 1.8; no less than 1.9; no less than 2.0; no less than 2.1; or no less than 2.2. In various instances, exemplary reformer output streams may comprise a hydrogen (H2) / carbon monoxide (CO) ratio may be no greater than 2.2; no greater than 2.1; no greater than 2.0; 1.9; 1.8; or 1.7.

[0036] Exemplary Fischer-Tropsch reactor input streams may comprise carbon monoxide (CO) and hydrogen (H2). Exemplary Fischer-Tropsch reactor input streams may further comprise steam (H2O).

[0037] Exemplary Fischer-Tropsch reactor output streams may comprise hydrocarbon products. Exemplary hydrocarbon products may comprise liquid fuel hydrocarbon material and lighter hydrocarbon material. Exemplary liquid hydrocarbon material may comprise C5to C64hydrocarbons. Further, exemplary liquid fuel hydrocarbon material may comprise kerosene, naphtha, waxes, liquid paraffin, lubricants, synthetic diesel, gasoline, or jet fuel. Exemplary lighter hydrocarbon material may comprise C1to C4hydrocarbons. III. Exemplary Systems

[0038] Various systems for processing natural gas and generating liquid fuel hydrocarbon material may be used to perform exemplary methods and techniques described herein. Various aspects of exemplary reactor systems are described below.

[0039] FIG. 1 schematically depicts an exemplary reactor system 100. System 100 may be particularly suited for processing natural gas and generating liquid fuel hydrocarbon material. As shown, exemplary system 100 comprises a reformer reactor 110, a heat exchange unit 120, aAttorney Docket No.029784-0011-WO01 Fischer-Tropsch reactor 130, a reformer reactor input stream 112, reformer reactor output stream 114, heat exchange output stream 124, Fischer-Tropsch reactor output stream 134, heated steam (H2O) stream 126, wherein heat exchange unit 120 comprises a plurality of inputs 122 and a plurality of outputs 128. Other embodiments may include more or fewer components.

[0040] Exemplary reformer reactor 110 is configured to perform various reactions, such as reacting carbon dioxide (CO2), steam (H2O), and natural gas (CH4) to generate hydrogen (H2) and carbon monoxide (CO). In some instances, reformer reactor 110 may comprise a multi-tubular catalytic bed. Reformer reactor 110 is in fluid communication with heat exchange unit 120.

[0041] Reformer reactor 110 is configured to receive reformer reactor input stream 112. Additional details regarding exemplary reformer reactor input streams are provided above.

[0042] Exemplary heat exchange unit 120 is configured to transfer heat generated in various components to various streams. In some instances, heat exchange unit 120 may comprise multiple heat exchange units. Heat exchange unit 120 may be configured in various ways. For example, heat exchange unit 120 may comprise multi-tubular heat exchangers. Other heat exchange configurations are contemplated.

[0043] Heat exchange unit 120 is configured to receive reformer reactor output stream 114 and to generate heat exchange output stream 124. Heat exchange unit 120 is in fluid communication with Fisher-Tropsch reactor 130.

[0044] Exemplary Fisher-Tropsch reactor 130 is configured to perform various reactions, such as reacting hydrogen (H2) and carbon monoxide (CO) to generate light hydrocarbon material and liquid fuel. In some instances, Fisher-Tropsch reactor 130 may comprise a multi- tubular catalytic bed, wherein the catalytic bed may comprise catalysts such as iron, cobalt, nickel, and ruthenium. An exemplary reaction in the Fisher-Tropsch reactor may be represented by Equation 2, shown above.

[0045] Fisher-Tropsch reactor 130 is configured to receive heat exchange output stream 124 and to generate Fischer-Tropsch reactor output stream 134. Fisher-Tropsch reactor 130 may have one or more inlets and one or more outlets.

[0046] FIG.2, FIG.3, and FIG.4 show embodiments of exemplary reactor systems 200, 300, and 400, respectively. In FIG.2, FIG.3, and FIG.4, dashed lines represent heat flow, solid lines represent material flow, dotted lines represent water (H2O) flow, and shaded boxes represent heat exchange units. Unless otherwise indicated, and for the sake of conciseness, likeAttorney Docket No.029784-0011-WO01 numbered reference numerals in FIG.3 and FIG. 4 perform like functions to those shown in FIG. 2. For example, Fischer-Tropsch reactor 230 in FIG. 2 performs a similar function to Fisher- Tropsch reactor 330 in FIG.3 and Fisher-Tropsch reactor 430 in FIG. 4.

[0047] FIG.2 schematically depicts an embodiment of exemplary reactor system 200. System 200 is suited for processing natural gas and generating liquid fuel hydrocarbon materials. As shown, exemplary system 200 comprises reformer reactor 210, Fischer-Tropsch reactor 230, separation unit 240, heater unit 250, heater unit 260, and heat exchange units 221, 223, 270, 280, 290, 294, and 296. Also shown is downstream process 278. Other embodiments may include more or fewer components.

[0048] In the embodiment shown, reformer reactor 210 is configured to receive heated reformer reactor input stream 212 from heat exchange unit 280 and heated steam (H2O) stream 274 from heat exchange unit 270. Reformer reactor 210 is configured to receive heat from heater unit 250. Reformer reactor 210 is configured to generate reformer reactor output stream 214. Reformer reactor 210 is in fluid communication with heat exchange unit 221.

[0049] Heat exchange unit 221 is configured to receive reformer reactor output stream 214. Heat exchange unit 221 is configured to generate a cooled reformer reactor output stream. Heat exchange unit 221 is configured to transfer heat. Heat exchange unit 221 is in fluid communication with heat exchange unit 223.

[0050] Heat exchange unit 223 is configured to receive cooling fluid 225. Heat exchange unit 223 is configured to receive cooled reformer reactor output stream from heat exchange unit 221. Heat exchange unit 223 is configured to generate a water stream 226 from condensed steam in the cooled reformer reactor output stream 224. Heat exchange unit 223 is in fluid communication with Fischer-Tropsch reactor 230.

[0051] Fischer-Tropsch reactor 230 is configured to receive cooled reformer reactor output stream 224. Fischer-Tropsch reactor 230 is configured to generate Fischer-Tropsch reactor output stream 234. Fischer-Tropsch reactor 230 is in fluid communication with separation unit 240.

[0052] Separation unit 240 is configured to separate gaseous and liquid hydrocarbon streams.

[0053] Separation unit 240 is configured to receive Fischer-Tropsch reactor output stream 234. Separation unit 240 is configured to generate light hydrocarbon material stream 242. Separation unit 240 is configured to generate liquid fuel stream 244. Separation unit 240 is in fluidAttorney Docket No.029784-0011-WO01 communication with heater unit 260.

[0054] Heater unit 260 is configured to receive light hydrocarbon material stream 242 and heated air stream 262. Heater unit 260 is configured to generate heater unit output stream 264. Heater unit 260 is in fluid communication with heat exchange unit 294.

[0055] Heat exchange unit 294 receives heater unit output stream 264. Heat exchange unit 294 is configured to transfer heat.

[0056] Heater unit 250 is configured to receive heated air stream 252 and to receive heated fuel stream 254. Heater unit 250 is configured to generate heater unit output stream 256. Heater unit 250 is configured to generate heat. Heater unit 250 is in fluid communication with heat exchange unit 296.

[0057] Heat exchange unit 296 is configured to receive heater unit output stream 256. Heat exchange unit 296 is configured to transfer heat.

[0058] Heat exchange unit 290 is configured to receive air stream 292. Heat exchange unit 290 is configured to exchange heat between heat exchange units 294 and 296. Heat exchange unit 290 is configured to generate heated air stream 252. Heat exchange unit 290 is in fluid communication with heater unit 250.

[0059] Heat exchange unit 270 is configured to receive cooling water stream 272. Heat exchange unit 270 is configured to exchange heat with heat exchange unit 221. Heat exchange unit 270 is configured to generate heated steam (H2O) streams 274 and 276.

[0060] Heated steam (H2O) stream 276 can be used for a downstream process 278. In some instances, downstream process 278 may comprise electricity generation or high-pressure steam production.

[0061] Heat exchange unit 280 is configured to provide reformer reactor input streams 212. Heat exchange unit 280 is configured to receive heat from heat exchange units 221 and 294. Heat exchange unit 280 is configured to generate heated reformer reactor input streams. Heat exchange unit 280 is in fluid communication with reformer reactor 210.

[0062] FIG.3 schematically depicts an embodiment of exemplary reactor system 300. System 300 is suited for processing natural gas and generating liquid fuel hydrocarbon materials. As shown, exemplary system 300 comprises reformer reactor 310, Fischer-Tropsch reactor 330, separation unit 340, heater unit 350, heater unit 360, and heat exchange units 321, 323, 370, 380, 390, 395, and 396. Also shown is downstream process 378. Other embodiments may include moreAttorney Docket No.029784-0011-WO01 or fewer components.

[0063] Reformer reactor 310 is configured to receive reformer reactor input stream 312, heated steam (H2O) stream 374, and light hydrocarbon material stream 346. Reformer reactor 310 is configured to generate reformer reactor output stream 314. Reformer reactor 310 is in fluid communication with heat exchange unit 321 and provides reformer reactor output stream 314 to heat exchange unit 321.

[0064] Heat exchange unit 395 is configured to exchange heat with heat exchange unit 321. Heat exchange unit 395 is configured to receive light hydrocarbon material stream 342. Heat exchange unit 395 is configured to generate heated light hydrocarbon material stream 346.

[0065] FIG.4 schematically depicts an embodiment of exemplary reactor system 400. System 400 is suited for processing natural gas and generating liquid fuel hydrocarbon materials. As shown, exemplary system 400 comprises reformer reactor 410, Fischer-Tropsch reactor 430, separation unit 440, heater unit 450, heater unit 460, and heat exchange units 421, 423, 470, 480, 490, 496, and 497. Also shown is downstream process 478. Other embodiments may include more or fewer components.

[0066] Heater unit 450 is configured to receive heated air stream 452 and fuel stream 454. Heater unit 450 is configured to receive heated light hydrocarbon material stream 448. Heater unit 450 is configured to generate heater unit output stream 456. Heater unit 450 is configured to generate heat. Heater unit 450 is in fluid communication with heat exchange unit 497.

[0067] Heat exchange unit 497 is configured to exchange heat with heat exchange unit 421. Heat exchange unit 497 is configured to receive light hydrocarbon material stream 442. Heat exchange unit 497 is configured to generate heated light hydrocarbon material stream 448.

[0068] FIG. 5 is a schematic, side sectional view of an embodiment of exemplary reactor system 500. Reactor system 500 is shown as an integrated, vertically arranged system. The embodiment shown in FIG. 5 may enable portability of reactor system 500, which may enable reactor system 500 to be used and transported among multiple locations where natural gas is produced.

[0069] As shown, reformer reactor 510 portion is disposed above a heat exchange 520 portion, and heat exchange unit 520 portion is disposed above Fischer-Tropsch reactor 530 portion.

[0070] Heat exchange unit 520 comprises a first heat exchange unit 522, a second heat exchange unit 524, and a third heat exchange 526. Heat exchange units 522 is disposed above heatAttorney Docket No.029784-0011-WO01 exchange unit 526, which is disposed above heat exchange unit 524. Heat exchange units 522, 524, and 526 are disposed above a Fischer-Tropsch reactor 530. The schematic shown in FIG.5 further depicts exemplary material flows.

[0071] As shown in FIG. 5, a heater unit surrounds reformer reactor 510 and the output from the heater unit is provided to heat exchange unit 526. Reformer reactor 510 receives reformer reactor inputs near a headspace of the reactor.

[0072] The reformer reactor 510 output flows to heat exchange unit 522. In heat exchange unit 522, the reformer reactor 510 output is used to heat various streams. As shown, the reformer reactor 510 output heats steam (H2O), ambient carbon dioxide (CO2), and ambient stranded natural gas. Heat exchange unit 522 includes a water knockout whereby condensed water from the reformer reactor 510 output is removed.

[0073] Heat exchange unit 526 receives ambient air and heating gas from the heater unit in reformer reactor 510. After being heated in heat exchange unit 526, heated air is provided to heat exchange unit 524 for additional heating.

[0074] Flue gas from light end flaring is used as the heating medium in heat exchange unit 524. As shown, flue gas in heat exchange unit 524 heats carbon dioxide (CO2) received from heat exchange unit 522. As shown, flue gas in heat exchange unit 524 also heats stranded natural gas received from heat exchange unit 522. As shown, flue gas in heat exchange unit 524 also heats air received from heat exchange unit 526.

[0075] Fischer-Tropsch reactor 530 receives reformer reactor output from heat exchange unit 522 (shown as high quality syngas). A cooling fluid may be used to remove exothermic heat from the Fischer-Tropsch reactor 530. As shown, cooling water is used, and resulting steam may be further heated in heat exchange unit 522 and provided to reformer reactor 510 and / or used for power generation. Fischer-Tropsch reactor 530 generates a light hydrocarbon material and a liquid fuel, which may be further processed and / or separated in one or more downstream operations, not shown in FIG.5.

[0076] FIG. 6 is a schematic, side sectional view of an embodiment of exemplary reactor system 600. Reactor system 600 is shown as an integrated, vertically arranged system. The embodiment shown in FIG. 6 may enable portability of reactor system 600, which may enable reactor system 600 to be used and transported among multiple locations where natural gas isAttorney Docket No.029784-0011-WO01 produced.

[0077] As shown, reformer reactor 610 portion is arranged as a catalytic, fixed bed reactor. Reformer reactor 610 portion is disposed above a heat exchange 620 portion, and heat exchange unit 620 portion is disposed above Fischer-Tropsch reactor 630 portion.

[0078] As shown in FIG.6, a heater unit surrounds a reformer reactor 610. In some instances, hot flue gas from the heater unit may be used for power generation. The heater unit may receive a light hydrocarbon material stream.

[0079] FIG. 6 depicts separation unit 640, or a flash drum, that receives Fischer-Tropsch reactor output. Separation unit 640 generates a light hydrocarbon material stream and a liquid fuel stream.

[0080] FIG. 6 depicts a heat exchange unit that receives a light hydrocarbon material stream. The heat exchange unit transfers heat that may be used for power generation. IV. Exemplary Methods of Operation

[0081] FIG. 7 schematically depicts exemplary method 700 of operating a reactor system. As shown, exemplary method 700 comprises: heating a reformer reactor using air and fuel (operation 704), providing a reformer reactor input stream to a reformer reactor (operation 708), collecting a reformer reactor output stream (operation 712), providing a reformer reactor output stream to a heat exchange unit (operation 716), collecting a first heat exchange output stream (operation 720), providing a heat exchange output stream to a Fischer-Tropsch reactor (operation 724), and collecting a Fischer-Tropsch reactor out stream (operation 728). Various systems may be used to implement method 700, such as systems 100 – 600 as shown in FIGS. 1-6. Other embodiments may include more or fewer operations.

[0082] Method 700 may begin by heating a reformer reactor (operation 704). Air may be heated air generated from a heat exchange unit. Stranded natural gas and / or a light hydrocarbon material stream may be reacted with air or heated air to heat a reformer reactor. In some instances, heated stranded natural gas and / or a heated light hydrocarbon material stream may be reacted with air or heated air.

[0083] Reformer reactor may be heated (operation 704) to operating temperatures between 900 °C and 1100 °C. In various instances, reformer reactor operating temperatures may be between 900 °C and 1100 °C; 950 °C and 1100 °C; 1000 °C and 1100 °C; 1050 °C and 1100 °C; 900 °CAttorney Docket No.029784-0011-WO01 and 1050 °C; 900 °C and 1000 °C; or 900 °C and 950 °C. In various instances, reformer reactor operating temperatures may be no less than 900 °C; no less than 950 °C; no less than 1000 °C; no less than 1050 °C; or no less than 1100 °C. In various instances, reformer reactor operating temperatures may be no greater than 1100 °C; no greater than 1050 °C; no greater than 1000 °C; no greater than 950 °C; or no greater than 900 °C.

[0084] Method 700 comprises providing a reformer reactor input stream to the reformer reactor (operation 708). Example reformer reactor input streams are described in greater detail above. Reformer input streams may be a temperature T1or preheated to a temperature T2whereby T2T1. The reformer reactor input streams may be provided to a single inlet or multiple inlets of a reformer reactor. The one or more inlets or outlets may be physically located on a top or upper portion of the reactor, at a side portion or a plurality of side locations, or near a bottom portion.

[0085] Method 700 comprises collecting a reformer reactor output stream (operation 712). The reformer reactor operates at a temperature T3, and the reformer reactor output stream is at a temperature T3. The reformer reactor output streams may comprise carbon monoxide (CO) and hydrogen (H2) and are described in greater detail above. The reformer reactor output streams may further comprise steam (H2O).

[0086] Method 700 comprises providing a reformer reactor output stream to a heat exchange unit (operation 716). In some instances, operation 712 and operation 716 occur simultaneously, as the reformer reactor output stream flows directly from the reformer reactor to the heat exchange unit. Method 700 comprises collecting a heat exchange output stream (operation 720). The heat exchange output stream may comprise cooled reformer reactor output stream of a temperature T4, where T4T3.

[0087] The reformer reactor output stream may provide heat to one or more streams in the heat exchange unit. For instance, method 700 may comprise providing carbon dioxide (CO2) input stream to the heat exchange unit and collecting a heated carbon dioxide (CO2) output stream from the heat exchange unit. Method 700 may comprise providing a steam (H2O) stream to the heat exchange unit and collecting a heated steam (H2O) stream from the heat exchange unit. Method 700 may comprise providing a stranded natural gas stream to a heat exchange unit and collecting a heated stranded natural gas stream from the heat exchange unit. As used herein, “heated” means the temperature of the stream exiting the heat exchange unit is great than the temperature of theAttorney Docket No.029784-0011-WO01 stream entering the heat exchange unit.

[0088] Method 700 comprises providing a heat exchange output stream comprising the cooled reformer reactor output stream to a Fischer-Tropsch reactor (operation 724). The Fischer-Tropsch reactor operates at a temperature T5, where T5T4or T5T4. The Fischer-Tropsch reactor input streams may be provided to a single inlet or multiple inlets of a Fischer-Tropsch reactor. The one or more inlets or outlets may be physically located on a reactor at a top or upper portion of the reactor, at a side portion or a plurality of side locations, or near a bottom portion.

[0089] Method 700 comprises collecting Fischer-Tropsch reactor output stream, where the Fischer-Tropsch reactor output stream is at a temperature, T5. Fischer-Tropsch reactor output stream comprises light hydrocarbon material stream and liquid fuel stream.

[0090] Operation 724 comprises providing heat exchange output stream to a Fischer-Tropsch reactor, which is configured to perform various reactions. Fischer-Tropsch reactor operating temperatures may be between 240 °C and 350 °C. In various instances, Fischer-Tropsch reactor operating temperatures may be between 240 °C and 350 °C; 275 °C and 350 °C; 300 °C and 350 °C; 325 °C and 350 °C; 240 °C and 325 °C; 240 °C and 300 °C; or 240 °C and 275 °C. In various instances, Fischer-Tropsch reactor operating temperatures may be no less than 240 °C; no less than 275 °C; no less than 300 °C; no less than 325 °C; or no less than 350 °C. In various instances, Fischer-Tropsch reactor operating temperatures may be no greater than 350 °C; no greater than 325 °C; no greater than 300 °C; no greater than 275 °C; or no greater than 240 °C.

[0091] Fischer-Tropsch reactor operating pressures may be between 2 MPa and 4 MPa. In various instances, Fischer-Tropsch reactor operating pressures may be between 2 MPa and 4 MPa; 2.4 MPa and 4 MPa; 2.8 MPa and 4 MPa; 3.2 MPa and 4 MPa; 3.6 MPa and 4 MPa; 2 MPa and 3.6 MPa; 2 MPa and 3.2 MPa; 2 MPa and 2.8 MPa; or 2 MPa and 2.4 MPa. In various instances, Fischer-Tropsch reactor operating pressures may be no less than 2 MPa; no less than 2.4 MPa; no less than 2.8 MPa; no less than 3.2 MPa; no less than 3.6 MPa; or no less than 4 MPa. In various instances, Fischer-Tropsch reactor operating pressures may be no greater than 4 MPa; no greater than 3.6 MPa; no greater than 3.2 MPa; no greater than 2.8 MPa; no greater than 2.4 MPa; or no greater than 2 MPa.

[0092] Method 700 may comprise providing cooling water to the Fischer-Tropsch reactor to absorb heat from the exothermic reactions and collecting steam (H2O) from the Fischer-Tropsch reactor. That is, the steam provided to the Fischer-Tropsch reactor is separated from with theAttorney Docket No.029784-0011-WO01 reactor reactants and products. The steam (H2O) stream provided to the heat exchange unit comprises the steam (H2O) from the Fischer-Tropsch reactor.

[0093] Method 700 may comprise providing a flue gas stream to a second heat exchange unit and collecting a cooled flue gas stream from the second heat exchange unit. That is, the flue gas stream may be used to provide heat to one or more streams.

[0094] Method 700 may comprise providing a heated carbon dioxide (CO2) output stream to the second heat exchange unit. Method 700 may comprise collecting a second heated carbon dioxide (CO2) output stream from the second heat exchange unit, where carbon dioxide (CO2) provided to the reformer reactor comprises the second heated carbon dioxide (CO2) output stream.

[0095] Method 700 may comprise providing a heated stranded natural gas stream to the second heat exchange unit, and collecting a second heated stranded natural gas stream from the second heat exchange unit. The natural gas (CH4) provided to the reformer reactor comprises the second heated stranded natural gas stream.

[0096] Method 700 may comprise providing heating gas generated in the reformer reactor to a third heat exchange unit and collecting cooled heating gas from the third heat exchange unit. That is, the heating gas may be used to heat one or more other streams in the third heat exchange unit. For instance, method 700 may comprise providing ambient air to the third heat exchange unit and collecting heated air from the third heat exchange unit. Method 700 may comprise providing heated air from the third heat exchange unit to a second heat exchange unit, and collecting second heated air from the second heat exchange unit.

[0097] Method 700 may comprise providing a heated steam (H2O) stream from the heat exchange unit to a power generation unit.

[0098] Method 700 may comprise providing a cooling fluid to the fourth heat exchange unit and providing a first heat exchange output stream comprising carbon monoxide (CO) and hydrogen (H2) to a fourth heat exchange unit, where the first heat exchange output stream additionally comprises steam (H2O). Method 700 may further comprise collecting a water stream from the fourth heat exchange unit, the water being condensed steam from the first heat exchange output stream.

[0099] Method 700 may comprise providing the Fischer-Tropsch reactor output stream to a separation unit, collecting a light hydrocarbon material stream from the separation unit, andAttorney Docket No.029784-0011-WO01 collecting a liquid fuel stream from the separation unit. V. Computational Data

[0100] Exemplary computational examples were generated, and the results are discussed below.

[0101] A computational version of the reactor system represented in FIG. 2 was simulated using Aspen Plus software. FIGS. 8A-11B show the system used for the computational simulations. The material balance for case 1 (FIG.2) is summarized in Table 1, and reactor details are presented in Table 3. Exemplary reactor system results are presented in Table 2.

[0102] Observations from Aspen simulations are summarized in Table 2.

[0103] Different heat integration strategies and reactor configurations were analyzed through system-level thermodynamic studies. Technoeconomic analysis compared the economic viability of each configuration. Bayesian optimization was then used to compare modular reactor designs for stranded natural gas utilization.Attorney Docket No.029784-0011-WO01

[0104] Table 1: Material Balance for Case 1 as presented in FIG. 2.Table 2. Process summary for different exemplary modular reactor configurations.Attorney Docket No.029784-0011-WO01 Table 3. Exemplary estimates for the design of a modular unit.Embodiments: For reasons of completeness, the following Embodiments are provided. Embodiment 1. A method for operating a reactor system comprising a reformer reactor, a heat exchange unit, and a Fischer-Tropsch reactor, the method comprising: heating the reformer reactor using air and fuel; providing a reformer reactor input stream to the reformer reactor, the reformer reactor input stream comprising natural gas (CH4), carbon dioxide (CO2), and steam (H2O); collecting a reformer reactor output stream generated in the reformer reactor from a reformer reactor outlet, the reformer reactor output stream comprising carbon monoxide (CO) and hydrogen (H2); providing the reformer reactor output stream to a first input of the heat exchange unit, collecting a first heat exchange output stream from a heat exchange unit outlet, the first heat exchange output stream comprising carbon monoxide (CO) and hydrogen (H2); and the first heat exchange output stream having a lower temperature than the reformer reactor output stream; providing the first heat exchange output stream to the Fischer-Tropsch reactor; collecting a Fischer-Tropsch reactor output stream from the Fischer-Tropsch reactor, the Fischer-Tropsch reactor output stream comprising hydrocarbon products.Attorney Docket No.029784-0011-WO01 Embodiment 2. The method according to Embodiment 1, where heating the reformer reactor comprises operating the reformer reactor at a temperature between 900 °C and 1100 °C. Embodiment 3. The method according to Embodiment 1 or Embodiment 2, the fuel comprising stranded natural gas; and wherein the natural gas in the reformer reactor input stream is stranded natural gas. Embodiment 4. The method according to any one of Embodiments 1-3, further comprising: providing a carbon dioxide (CO2) input stream to the heat exchange unit; collecting a heated carbon dioxide (CO2) output stream from the heat exchange unit; providing a steam (H2O) stream to the heat exchange unit; collecting a heated steam (H2O) stream from the heat exchange unit; providing a stranded natural gas stream to the heat exchange unit; and collecting a heated stranded natural gas stream from the heat exchange unit. Embodiment 5. The method according to Embodiment 4, where the carbon dioxide (CO2) provided to the reformer reactor comprises the heated carbon dioxide (CO2) output stream; where the steam (H2O) provided to the reformer reactor comprises the heated steam (H2O) stream; where the natural gas (CH4) provided to the reformer reactor comprises the heated stranded natural gas stream. Embodiment 6. The method according to Embodiment 4 or Embodiment 5, further comprising: providing cooling water to the Fischer-Tropsch reactor; collecting steam (H2O) from the Fischer- Tropsch reactor, where the steam (H2O) stream provided to the heat exchange unit comprises the steam (H2O) from the Fischer-Tropsch reactor. Embodiment 7. The method according to any one of Embodiments 4-6, further comprising: providing a flue gas stream to a second heat exchange unit; collecting a cooled flue gas stream from the second heat exchange unit; providing the heated carbon dioxide (CO2) output stream to the second heat exchange unit; collecting a second heated carbon dioxide (CO2) output stream from the second heat exchange unit, where the carbon dioxide (CO2) provided to the reformer reactor comprises the second heated carbon dioxide (CO2) output stream; providing the heatedAttorney Docket No.029784-0011-WO01 stranded natural gas stream to the second heat exchange unit; collecting a second heated stranded natural gas stream from the second heat exchange unit, where the natural gas (CH4) provided to the reformer reactor comprises the second heated stranded natural gas stream. Embodiment 8. The method according to Embodiment 7, further comprising: providing heating gas generated in the reformer reactor to a third heat exchange unit; collecting cooled heating gas from the third heat exchange unit; providing ambient air to the third heat exchange unit; collecting heated air from the third heat exchange unit; providing the heated air to the second heat exchange unit; collecting second heated air from the second heat exchange unit. Embodiment 9. The method according to Embodiment 7, further comprising: providing the heated steam (H2O) stream from the heat exchange unit to a power generation unit. Embodiment 10. The method according to any one of Embodiments 4-9, further comprising: providing the first heat exchange output stream comprising carbon monoxide (CO) and hydrogen (H2) to a fourth heat exchange unit, where the first heat exchange output stream additionally comprises steam (H2O); providing a cooling fluid to the fourth heat exchange unit; collecting a water stream from the fourth heat exchange unit, the water stream being condensed steam from the first heat exchange output stream; and providing the carbon monoxide (CO) and hydrogen (H2) to the Fischer-Tropsch reactor. Embodiment 11. The method according to any one of Embodiments 1-10, further comprising: providing the Fischer-Tropsch reactor output stream to a separation unit; collecting a light hydrocarbon material stream from the separation unit; and collecting a liquid fuel stream from the separation unit. Embodiment 12. A reactor system, comprising: a reformer reactor comprising: a reformer reactor inlet in fluid communication with a reformer reactor input stream source and configured to receive the reformer reactor input stream, the reformer reactor input stream comprising natural gas (CH4), carbon dioxide (CO2), and steam (H2O); a reformer reactor outlet configured to provide a reformer reactor output stream, the reformer reactor output stream comprising carbonAttorney Docket No.029784-0011-WO01 monoxide (CO) and hydrogen (H2); a heat exchange unit comprising a plurality of inlets and a plurality of outlets, the heat exchange unit configured to: increase a temperature of a plurality of input streams with the reformer reactor output stream, the plurality of input streams comprising a steam stream, a carbon dioxide (CO2) stream, and a natural gas (CH4) stream; decrease a temperature of the reformer reactor output stream; collect water condensed from the reformer reactor output stream; wherein one of the plurality of outlets comprises a syngas outlet; a Fischer-Tropsch reactor comprising: a catalyst bed; a Fischer-Tropsch reactor inlet in fluid communication with the syngas outlet of the heat exchange unit and configured to distribute syngas over the catalyst bed and generate hydrocarbon products; a Fischer-Tropsch reactor outlet configured to provide the hydrocarbon products. Embodiment 13. The reactor system according to Embodiment 12, further comprising: a separation unit in fluid communication with the Fischer-Tropsch reactor outlet; the separation unit configured to separate liquid fuel and lighter hydrocarbon material in the hydrocarbon products. Embodiment 14. The reactor system according to Embodiment 12 or Embodiment 13, wherein the reformer reactor is disposed adjacent to the heat exchange unit; wherein the heat exchange unit is disposed adjacent to the Fischer-Tropsch reactor. Embodiment 15. The reactor system according to any one of Embodiments 12-14, the reactor system being vertically arranged such that the reformer reactor is disposed above the heat exchange unit and the heat exchange unit is disposed above the Fischer-Tropsch reactor. Embodiment 16. The reactor system according to any one of Embodiments 12-15, further comprising a first heater unit arranged to provide heat to the reformer reactor, the first heater unit configured to receive air and / or stranded natural gas. Embodiment 17. The reactor system according to Embodiment 16, further comprising a second heating unit in fluid communication with the separation unit and configured to receive the lighterAttorney Docket No.029784-0011-WO01 hydrocarbon material from the separation unit; the second heating unit arranged to provide heat to the carbon dioxide (CO2) stream and the natural gas (CH4) stream. Embodiment 18. The reactor system according to Embodiment 16 or Embodiment 17, further comprising a second heat exchange unit in fluid communication with the separation unit and configured to receive the lighter hydrocarbon material; the second heat exchange unit configured to receive heat from the heat exchange unit; and the second heat exchange unit in fluid communication with the first heater unit and configured to provide heated lighter hydrocarbon material to the first heater unit. Embodiment 19. The reactor system according to any one of Embodiments 12-18, further comprising a second heat exchange unit adjacent to the Fischer-Tropsch reactor and configured to receive heat from the Fischer-Tropsch reactor; the second heat exchange unit comprising a water inlet and a steam outlet; the steam outlet being in fluid communication with the reformer reactor. Embodiment 20. The reactor system according to Embodiment 18, wherein the steam outlet of the second heat exchange unit is in fluid communication with an electricity generation unit; or wherein the steam outlet of the second heat exchange unit is in fluid communication with a steam storage unit.

Claims

Attorney Docket No.029784-0011-WO01 CLAIMS 1. A method for operating a reactor system comprising a reformer reactor, a heat exchange unit, and a Fischer-Tropsch reactor, the method comprising: heating the reformer reactor using air and fuel; providing a reformer reactor input stream to the reformer reactor, the reformer reactor input stream comprising natural gas (CH4), carbon dioxide (CO2), and steam (H2O); collecting a reformer reactor output stream generated in the reformer reactor from a reformer reactor outlet, the reformer reactor output stream comprising carbon monoxide (CO) and hydrogen (H2); providing the reformer reactor output stream to a first input of the heat exchange unit, collecting a first heat exchange output stream from a heat exchange unit outlet, the first heat exchange output stream comprising carbon monoxide (CO) and hydrogen (H2); and the first heat exchange output stream having a lower temperature than the reformer reactor output stream; providing the first heat exchange output stream to the Fischer-Tropsch reactor; collecting a Fischer-Tropsch reactor output stream from the Fischer-Tropsch reactor, the Fischer-Tropsch reactor output stream comprising hydrocarbon products.

2. The method according to claim 1, where heating the reformer reactor comprises operating the reformer reactor at a temperature between 900 °C and 1100 °C.

3. The method according to claim 1, the fuel comprising stranded natural gas; and wherein the natural gas in the reformer reactor input stream is stranded natural gas.

4. The method according to claim 1, further comprising: providing a carbon dioxide (CO2) input stream to the heat exchange unit; collecting a heated carbon dioxide (CO2) output stream from the heat exchange unit; providing a steam (H2O) stream to the heat exchange unit;Attorney Docket No.029784-0011-WO01 collecting a heated steam (H2O) stream from the heat exchange unit; providing a stranded natural gas stream to the heat exchange unit; and collecting a heated stranded natural gas stream from the heat exchange unit.

5. The method according to claim 4, where the carbon dioxide (CO2) provided to the reformer reactor comprises the heated carbon dioxide (CO2) output stream; where the steam (H2O) provided to the reformer reactor comprises the heated steam (H2O) stream; where the natural gas (CH4) provided to the reformer reactor comprises the heated stranded natural gas stream.

6. The method according to claim 5, further comprising: providing cooling water to the Fischer-Tropsch reactor; collecting steam (H2O) from the Fischer-Tropsch reactor, where the steam (H2O) stream provided to the heat exchange unit comprises the steam (H2O) from the Fischer-Tropsch reactor.

7. The method according to claim 4, further comprising: providing a flue gas stream to a second heat exchange unit; collecting a cooled flue gas stream from the second heat exchange unit; providing the heated carbon dioxide (CO2) output stream to the second heat exchange unit; collecting a second heated carbon dioxide (CO2) output stream from the second heat exchange unit, where the carbon dioxide (CO2) provided to the reformer reactor comprises the second heated carbon dioxide (CO2) output stream; providing the heated stranded natural gas stream to the second heat exchange unit; collecting a second heated stranded natural gas stream from the second heat exchange unit, where the natural gas (CH4) provided to the reformer reactor comprises the second heated stranded natural gas stream.Attorney Docket No.029784-0011-WO01 8. The method according to claim 7, further comprising: providing heating gas generated in the reformer reactor to a third heat exchange unit; collecting cooled heating gas from the third heat exchange unit; providing ambient air to the third heat exchange unit; collecting heated air from the third heat exchange unit; providing the heated air to the second heat exchange unit; collecting second heated air from the second heat exchange unit.

9. The method according to claim 7, further comprising: providing the heated steam (H2O) stream from the heat exchange unit to a power generation unit.

10. The method according to claim 4, further comprising: providing the first heat exchange output stream comprising carbon monoxide (CO) and hydrogen (H2) to a fourth heat exchange unit, where the first heat exchange output stream additionally comprises steam (H2O); providing a cooling fluid to the fourth heat exchange unit; collecting a water stream from the fourth heat exchange unit, the water stream being condensed steam from the first heat exchange output stream; and providing the carbon monoxide (CO) and hydrogen (H2) to the Fischer-Tropsch reactor.

11. The method according to claim 1, further comprising: providing the Fischer-Tropsch reactor output stream to a separation unit; collecting a light hydrocarbon material stream from the separation unit; and collecting a liquid fuel stream from the separation unit.

12. A reactor system, comprising: a reformer reactor comprising: a reformer reactor inlet in fluid communication with a reformer reactor input stream source and configured to receive the reformer reactor input stream,Attorney Docket No.029784-0011-WO01 the reformer reactor input stream comprising natural gas (CH4), carbon dioxide (CO2), and steam (H2O); a reformer reactor outlet configured to provide a reformer reactor output stream, the reformer reactor output stream comprising carbon monoxide (CO) and hydrogen (H2); a heat exchange unit comprising a plurality of inlets and a plurality of outlets, the heat exchange unit configured to: increase a temperature of a plurality of input streams with the reformer reactor output stream, the plurality of input streams comprising a steam stream, a carbon dioxide (CO2) stream, and a natural gas (CH4) stream; decrease a temperature of the reformer reactor output stream; collect water condensed from the reformer reactor output stream; wherein one of the plurality of outlets comprises a syngas outlet; a Fischer-Tropsch reactor comprising: a catalyst bed; a Fischer-Tropsch reactor inlet in fluid communication with the syngas outlet of the heat exchange unit and configured to distribute syngas over the catalyst bed and generate hydrocarbon products; a Fischer-Tropsch reactor outlet configured to provide the hydrocarbon products.

13. The reactor system according to claim 12, further comprising: a separation unit in fluid communication with the Fischer-Tropsch reactor outlet; the separation unit configured to separate liquid fuel and lighter hydrocarbon material in the hydrocarbon products.

14. The reactor system according to claim 13, wherein the reformer reactor is disposed adjacent to the heat exchange unit; wherein the heat exchange unit is disposed adjacent to the Fischer-Tropsch reactor.

15. The reactor system according to claim 14, the reactor system being vertically arranged such that the reformer reactor is disposed above the heat exchange unit and the heat exchange unit is disposed above the Fischer-Tropsch reactor.Attorney Docket No.029784-0011-WO01 16. The reactor system according to claim 13, further comprising a first heater unit arranged to provide heat to the reformer reactor, the first heater unit configured to receive air and / or stranded natural gas.

17. The reactor system according to claim 16, further comprising a second heating unit in fluid communication with the separation unit and configured to receive the lighter hydrocarbon material from the separation unit; the second heating unit arranged to provide heat to the carbon dioxide (CO2) stream and the natural gas (CH4) stream.

18. The reactor system according to claim 16, further comprising a second heat exchange unit in fluid communication with the separation unit and configured to receive the lighter hydrocarbon material; the second heat exchange unit configured to receive heat from the heat exchange unit; and the second heat exchange unit in fluid communication with the first heater unit and configured to provide heated lighter hydrocarbon material to the first heater unit.

19. The reactor system according to claim 12, further comprising a second heat exchange unit adjacent to the Fischer-Tropsch reactor and configured to receive heat from the Fischer-Tropsch reactor; the second heat exchange unit comprising a water inlet and a steam outlet; the steam outlet being in fluid communication with the reformer reactor.

20. The reactor system according to claim 18, wherein the steam outlet of the second heat exchange unit is in fluid communication with an electricity generation unit; or wherein the steam outlet of the second heat exchange unit is in fluid communication with a steam storage unit.

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