CA3193997A1 - Systems and methods for converting captured co2 to naphtha - Google Patents

Abstract

There are provided systems and methods for converting captured carbon into naphtha, which can be used as a diluent for diluting heavy crude oil and bitumen. The captured carbon dioxide is provided as a feedstock along with methane for reforming to produce a synthesis gas. Hydrogen can be provided as a feedstock along with or in place of methane.
The synthesis gas is synthesized into methanol, which is used to synthesize naphtha to create a naphtha product such as a diluent. The methanol may be synthesized into dimethyl ether which is used to synthesize the naphtha.

Description

Systems and Methods for Converting Captured CO2 to Naphtha TECHNICAL FIELD
[0001] The disclosure relates to the production of hydrocarbon products, and more specifically to producing a naphtha from captured carbon.
BACKGROUND

[0002] In oil and gas operations, crude oils are often transported from the production field to refineries by pipeline. Heavy crude oil and bitumen, which are commonly produced in the Athabasca oil sands in Alberta, Canada, and Venezuela have high viscosity which prevents them from being transported efficiently by pipeline without first reducing their viscosity. Viscosity reduction is commonly accomplished by blending the heavy oil or bitumen with a diluent, which is typically a light hydrocarbon. Commonly used diluents include natural gas condensate, naphtha, and synthetic crude oil.

[0003] Natural gas condensate is a mixture of light liquid hydrocarbons (C3 to C6) that is typically separated out of a natural gas stream at the point of production, and includes natural gas liquids and naphtha. Naphtha is a light liquid hydrocarbon containing varying amounts of paraffins, olefins, naphthene constituents, and aromatics. Naphtha may also be obtained directly from crude oil by distillation or from other processes and products like refinery reformate, catalytic cracking, and delayed coker product distillation.

[0004] Large quantities of diluent need to be transported from refineries to well sites where heavy oil and bitumen are produced. A considerable amount of diluent is imported from the U.S. into Alberta to meet the demand for diluent.

[0005] The production and transportation of diluent results in greenhouse gas emissions, including carbon dioxide. This contributes to increased atmospheric concentrations of carbon dioxide, and therefore to global warming. An object of this invention is to produce diluent in a manner that is more environmentally friendly and reduces the net amount of carbon dioxide produced.

Date Recue/Date Received 2023-03-23 SUMMARY

[0006] In accordance with the disclosure, there are provided systems and methods for producing naphtha from captured carbon dioxide. The naphtha can be used as a diluent for reducing the viscosity of heavy crude oil or bitumen.

[0007] In some embodiments, the method for producing naphtha from captured carbon dioxide comprises the steps: a) providing feedstocks including methane and captured carbon dioxide; b) reforming the feedstocks to produce a synthesis gas comprising hydrogen, carbon monoxide and carbon dioxide; c) synthesizing methanol from the synthesis gas; and d) synthesizing naphtha from the methanol. The feedstocks may include hydrogen.

[0008] In some embodiments, the method for producing naphtha from captured carbon dioxide comprises the steps: a) providing feedstocks including hydrogen and captured carbon dioxide; b) reforming the feedstocks to produce a synthesis gas comprising hydrogen, carbon monoxide and carbon dioxide; c) synthesizing methanol from the synthesis gas; and d) synthesizing naphtha from the methanol.

[0009] The synthesis gas may comprise (H2 - CO2) / (CO + CO2) having a molar ratio of about 2.0 to about 2.1.

[0010] After step c), dimethyl ether may be synthesized from the methanol, and the dimethyl ether is used to synthesize the naphtha.

[0011] The feedstocks may include carbon dioxide captured from steam-assisted gravity drainage (SAGD) operations used in production of the heavy crude oil or bitumen. The feedstocks may include natural gas. The feedstocks may include biomethane. The feedstocks may include hydrogen derived from biomass, including biomass gasification and/or anaerobic digestion of biomass. The feedstocks may include hydrogen derived from reforming of natural gas.

[0012] The reforming in step b) may comprise steam methane reforming. The reforming may comprise autothermal reforming.

[0013] Synthesizing the naphtha may include removing light hydrocarbons Cl to C4.

Date Recue/Date Received 2023-03-23

[0014] In some embodiments, there is a system for producing naphtha from captured carbon dioxide comprising a source of methane; a source of captured carbon dioxide; a reformer for receiving the methane and captured carbon dioxide and producing synthesis gas; a methanol reactor for synthesizing methanol from the synthesis gas; a naphtha reactor for synthesizing naphtha from the methanol; and a fractionation or distillation unit for removing gaseous hydrocarbons from the naphtha. There may be a source of hydrogen for input into the reformer.

[0015] In some embodiments, there is a system for producing naphtha from captured carbon dioxide comprising: a source of hydrogen; a source of captured carbon dioxide; a reformer for receiving the hydrogen and captured carbon dioxide and producing synthesis gas; a methanol reactor for synthesizing methanol from the synthesis gas; a naphtha reactor for synthesizing naphtha from the methanol; and a fractionation or distillation unit for removing gaseous hydrocarbons from the naphtha.
BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Various objects, features and advantages of the disclosure will be apparent from the following description of particular embodiments, as illustrated in the accompanying drawings. The drawings are not necessarily to scale, emphasis instead being placed upon illustrating the principles of various embodiments of the invention. Similar reference numerals indicate similar components.
FIG. 1 is a flow chart showing one embodiment of a process for converting captured CO2 and methane to a naphtha-based diluent.
FIG. 2 is a flow chart showing one embodiment of a process for converting captured CO2 and hydrogen to a naphtha-based diluent.
FIG. 3 is a flow chart showing one embodiment of a process for converting captured CO2, methane and hydrogen to a naphtha-based diluent.
FIG. 4 is a flow chart showing one embodiment of the system for converting captured CO2 into a naphtha-based diluent.

Date Recue/Date Received 2023-03-23 FIG. 5 is a graph showing a typical distillation curve for naphtha.
DETAILED DESCRIPTION

[0017] The transportation of diluent to well sites where heavy oil and bitumen are produced leads to increased costs and greenhouse gas (GHG) emissions as a result of importing and transporting diluent over long distances. There is a need and desire to reduce GHG emissions to stop or slow climate change, and there is increasing regulation on GHG emissions, including carbon emissions in the oil and gas sector.
Various mechanisms to tax, price or otherwise set limitations on carbon emissions are increasing.

[0018] One method of reducing carbon emissions is to capture carbon dioxide (CO2), that would normally be emitted, for reuse, resulting in a growing industry of CO2 capture. There is a need for products and systems that are able to recycle and reuse the captured CO2, referred to as carbon capture and utilization (CCU).

[0019] The subject systems and methods provide a way to use captured CO2 by manufacturing a naphtha-based diluent from captured CO2 for adding to heavy crude oil and bitumen to reduce its viscosity and facilitate its transportation. Bitumen is extra-heavy hydrocarbon oil that has a density of less than 100 API. Heavy crude oil is typically defined as having a density of 10 API up to 21.50 API.

[0020] Every carbon atom that is recycled and reused from a captured CO2 molecule eliminates the need to having to produce that carbon atom from a fossil source. By producing diluent from captured CO2 (CCU), oil and gas producers are also able to decrease their net emission of CO2. In addition, if CO2 can be captured and transformed into diluent at the same location or nearby where the diluent is blended with heavy crude oil and bitumen, it eliminates or reduces the need to transport diluent to the site of use, further reducing CO2 emissions and costs associated with the transportation of diluent.

[0021] Various aspects of the invention will now be described with reference to the figures.
For the purposes of illustration, components depicted in the figures are not necessarily drawn to scale. Instead, emphasis is placed on highlighting the various contributions of the components to the functionality of various aspects of the invention. A
number of possible alternative features are introduced during the course of this description. It is to Date Recue/Date Received 2023-03-23 be understood that, according to the knowledge and judgment of persons skilled in the art, such alternative features may be substituted in various combinations to arrive at different embodiments of the present invention.

[0022] Synthesizing Naphtha from Methane

[0023] One embodiment of the subject method 10 is illustrated in FIG. 1, showing the method by which captured CO2 from a carbon source is used to prepare a naphtha-based diluent 26. First, methane (CH4) 14 and captured CO212 are reformed 18 with the addition of H20 16 to produce synthesis gas 20, commonly referred to as syngas which comprises hydrogen, carbon monoxide and carbon dioxide.

[0024] In some embodiments, the methane and captured CO2 are reformed 18 into syngas using steam methane reforming. In steam methane reforming, the methane 14 is reacted with high-temperature steam (H2O 16) in the presence of a catalyst to form the syngas 20. The reaction is:
CH4 + CO2 + H20 (+ heat) -> CO + 3H2 followed by a water-gas shift reaction:
CO + H20 -> CO2 + H2

[0025] In some embodiments, the methane and captured CO2 are reformed 18 into syngas using autothermal reforming. In autothermal reforming, oxygen and CO2 are reacted with methane to form the syngas 20 through partial oxidization of the methane.
The reaction is:
2CH4 + 02 + CO2 -> 2H2 + 3C0 + H20 (+ heat)

[0026] In autothermal reforming, steam can also be introduced in which case the following reaction occurs:
4CH4 + 02 + 2H20 (+ heat) -> 1 OH2 + 4C0 Date Recue/Date Received 2023-03-23

[0027] After the reforming step 18, the syngas is synthesized into methanol 22. The methanol 22 is then used to synthesize naphtha 24 which can then be used as a naphtha-based diluent 26.

[0028] In some embodiments, the methane is provided in the form of natural gas derived from fossil fuels.

[0029] In some embodiments, the methane is provided in the form of biomethane, which is derived from biomass and is a renewable energy source. Biomethane can be produced from organic household waste, dead animal and plant material, manure, waste activated sludge from wastewater treatment plans (both municipal and industrial), and other organic matter sources. The biomethane may come from anerobic digestion or from biomass gasification.

[0030] The methane may also come from a combination of natural gas and biomethane.

[0031] Synthesizing Naphtha from Hydrogen

[0032] In some embodiments, as in the example in FIG. 2, there is provided a method 30 for synthesizing naphtha using hydrogen 28 and captured CO2 12. This method 30 is similar to the method shown in FIG. 1, except that hydrogen 28 is used in place of methane as a feedstock for producing the syngas 20, and H20 is not required as a feedstock. The hydrogen can come from a number of suitable processes for producing hydrogen.
When hydrogen is used to form the syngas, it is not necessary to add H20 as a feedstock.

[0033] The hydrogen 28 may be produced from electrolysis, where electricity from a renewable or non-renewable source is used to split water into hydrogen and oxygen. The hydrogen may be produced from direct solar water splitting, where light energy is used to split water into hydrogen and oxygen.

[0034] The hydrogen 28 may be produced from biomass. One method for producing hydrogen from biomass is gasification, which is a controlled process involving heat, and possibly air or a steam and oxygen mix to convert biomass to hydrogen, carbon monoxide and carbon dioxide. The carbon monoxide then reacts with water to form CO2 and more Date Recue/Date Received 2023-03-23 hydrogen via a water-gas shift reaction, and the hydrogen is separated from the gas stream.

[0035] The hydrogen may be produced from biomass through microbial biomass conversion via anaerobic digestion, where microorganisms break down organic matter to produce hydrogen. This can be from direct hydrogen fermentation, where the microbes produce the hydrogen themselves by breaking down complex molecules through many different pathways, and the byproducts of some of the pathways can be combined by enzymes to produce hydrogen. Hydrogen can also be formed indirectly using microbial electrolysis cells.

[0036] The hydrogen may be produced from reforming fossil fuels, including natural gas, to release hydrogen. For example, hydrogen can be produced using steam methane reforming, described above, where a methane source, such as natural gas, is reacted with high-temperature steam in the presence of a catalyst to produce hydrogen, along with carbon monoxide and carbon dioxide.

[0037] The hydrogen can be produced from fossil fuels using autothermal reforming, as described above, where oxygen and CO2 or steam are reacted with methane in the hydrocarbon feed to form hydrogen and carbon monoxide through partial oxidization.

[0038] To reform the hydrogen 28 and captured CO2 12 into syngas 20, the following reaction occurs:
CO2 + 2H2 (+ heat) -> CO + H2 + CO2 + H20

[0039] The proportion of H2 is controlled to provide the desired syngas composition such that the syngas composition meets the ratio (H2 ¨ CO)/(CO2 + CO) = 2.0 to 2.1.

[0040] Once the syngas 20 is formed, the remaining steps of methanol synthesis 22 and naphtha synthesis 24 to produce a naphtha-based diluent 26 proceed in the same manner as for the embodiment in FIG. 1.

[0041] Naphtha Synthesis from Methane and Hydrogen Date Recue/Date Received 2023-03-23

[0042] In some embodiments, as in the example shown in FIG. 3, there is provided a method 40 for synthesizing naphtha from feedstocks comprising methane 14, hydrogen 28, and captured CO2 12. This method 40 is a combination of the previously described methods 10, 30. Instead of using a feedstock of only methane (FIG. 1) or only hydrogen (FIG. 2), a combination of methane 14 and hydrogen 28 are reformed with captured CO2 12 to produce syngas 20. In this case, H20 is also input into the reforming process, as in the method 10 in FIG. 1. The remaining steps of methanol synthesis 22 and naphtha synthesis 24 to form a naphtha-based diluent 26 remain the same.

[0043] The sources of methane and hydrogen may be any of the sources described above with reference to FIGS. 1, 2, or any other suitable sources.

[0044] Captured Carbon Sources

[0045] There may be one or more carbon source for the captured CO2 12 used in the methods 10, 30, 40. The carbon source can be at or near a production well site where the diluent end-product is to be used (i.e. where it is blended with heavy crude oil or bitumen), or it can be at a different location.

[0046] One source of captured carbon is steam-assisted gravity drainage (SAGD) facilities. SAGD is an enhanced oil recovery technology for producing heavy crude oil and bitumen that injects steam into an oil reservoir to heat the oil and reduce its viscosity, allowing the oil to drain into a well bore and be pumped out for recovery. CO2 is a byproduct of steam generation at SAGD facilities, and typically the CO2 is vented to the atmosphere.
In the subject system, the CO2 produced during SAGD operations is captured (instead of being vented to the atmosphere) and used as a feedstock. Since SAGD is used to produce heavy crude oil and bitumen, which requires diluent to be blended with it prior to transportation, capturing CO2 from SAGD facilities advantageously provides captured CO2 at or near the site that the naphtha-based diluent end product is used.

[0047] The subject methods can also use captured CO2 that is generated during various intermediate steps of the method 10, 30, 40, including during methane reforming 18, hydrogen reforming 28, methanol synthesis 22, and naphtha synthesis 24.

Date Recue/Date Received 2023-03-23

[0048] CO2 can be captured from processes for generating heat or electricity for the subject methods. For example, heat or electricity may be generated through the combustion of biomass or fossil fuels that are used for the reforming step 18.

[0049] The subject methods can use captured CO2 that is generated during methane and/or hydrogen production, for example during biomass gasification, anaerobic digestion of biomass, steam methane reforming and autothermal reforming.

[0050] In some embodiments, the subject methods use captured CO2 from sources that aren't directly part of the method itself. This includes, but is not limited to, upstream natural gas production, synthetic fertilizer production, cement production, and fermentation processes.

[0051] The captured carbon is preferably 99.5% pure CO2. In some embodiments, the captured CO2 may contain impurities that require additional steps for purging.
Certain impurities, such as light hydrocarbons (Cl to C4) would not require purging.

[0052] Sy n gas

[0053] The composition of the syngas 20 that is produced by the subject methods 10, 30, 40 is controlled by the feedstock ratios of captured CO2, methane, hydrogen, and water.

[0054] The syngas preferably comprises carbon monoxide, hydrogen and carbon dioxide having the following ratio:
(H2 - CO2) / (CO + CO2) in a molar ratio of about 2.0 to about 2.1.

[0055] The desired ratio of about 2.0 to about 2.1 is obtained by adjusting the feedstock ratios.

[0056] When the syngas is reformed from a feedstock generated from biomass, the syngas is commonly referred to as bio-syngas.

[0057] In some embodiments, the ratio for reforming methane to form a syngas having a suitable ratio for methanol synthesis is:
3CH4 + CO2 + H20 -> 4C0 + 8H2 Date Recue/Date Received 2023-03-23

[0058] One suitable composition for feedstock streams to reform syngas is provided in Table 1 below, wherein the input streams are natural gas, natural gas fuel and captured carbon dioxide. The natural gas fuel is used to provide heat-energy for the reforming.

[0059] Table 1. Properties and composition of input and output streams for reforming syngas.
Natural Gas Natural Gas Capture CO2 Produced Feed Fuel Feed Stream Syngas Property Temperature 40.0 40.0 129.2 38 ( C) Pressure (barg) 32 32 30 16 Molar Flow Rate 938 408.2 252 3634 (kgmol/h) Mass Flow Rate 15,624 6,802.5 11,090 41,581 (kg/h) Mole Fraction CO2 0.0100 0.0100 1.0000 0.0724 CO - - - 0.2223 H2 - - - 0.6637 H20 - - - 0.0037 N2 0.0050 0.0050 - 0.0013 CH4 0.9700 0.9700 - 0.0366 C2H6 0.0100 0.0100 - -C3H8 0.0050 0.0050 - -

[0060] When methane is reformed, the process requires H20 16 as a feedstock in the form of steam to provide heat and additional 02. H20 is a byproduct of the process, including during naphtha synthesis when methanol is converted to naphtha.
Therefore the H20 is preferably sourced from the process itself. The amount of H20 16 is adjusted Date Recue/Date Received 2023-03-23 subject to the ratios of captured CO2, methane, and hydrogen to produce a syngas with the desired composition.

[0061] Methanol Synthesis

[0062] The syngas is used to synthesize methanol 22 using a suitable process, such as catalytic conversion of hydrogen and carbon monoxide with conventional gas-phase processes or with a liquid phase methanol process. The methanol synthesis reactions include:
2H2 + CO ¨> CH3OH
CO2 + 3H2 -> CH3OH + H20 CO + H20 -> CO2 + H2

[0063] The latter reaction is the water-gas shift reaction, which occurs to provide the necessary H2/C0 ratio for full conversion to methanol.

[0064] Conventional gas-phase processes typically carry out the conversion to methanol in fixed-bed reactors at high pressure, for example from about 600 to about 1,700 psig at about 200 to 315 C. Suitable catalysts generally comprise one or more of copper, zinc oxide, alumina and magnesia. An alternative catalyst may comprise carbon, nitrogen and platinum.

[0065] In some embodiments, dimethyl ether (DME) (CH3OCH3) is synthesized from methanol before being converted to naphtha by way of the reaction:
2CH3OH -> CH3OCH3+ H20

[0066] In some embodiments, DME is synthesized directly from the syngas before being converted to naphtha, skipping the methanol synthesis step 22.

[0067] Naphtha Synthesis

[0068] After methanol or DME synthesis, the methanol and/or DME is synthesized into naphtha 24 using suitable processes. The reaction paths include:
CH3OCH3 and/or CH3OH -> Light Olefins + H20 Date Recue/Date Received 2023-03-23 Light Olefins -> CH5 + Olefins C5 + Olefins -> Paraffins + Naphthenes + Aromatics

[0069] One suitable process is a methanol-to-gasoline (MTG) process developed by ExxonMobilTm, wherein methanol is vaporized and superheated through a series of heat exchangers, then fed into a fluid bed reactor for conversion to hydrocarbons and water. In the reactor, light olefins oligomerize into higher olefins, which combine through various reaction paths into paraffins, naphthenes and methylated aromatics.

[0070] Another suitable process is Ha!dor Topose's TIGASTm (Topsoe Improved Gasoline Synthesis) process.

[0071] The hydrocarbon product from MTG processes generally comprises hydrocarbons in the Cl to C10 range, and even up to the C12 range. The lighter components in the Cl to C4 range are gaseous at normal temperature and pressure, and are separated out by simple distillation. The remaining hydrocarbons are generally in the naphtha range of C5 to C10, and are usable as a naphtha-based diluent to be blended with heavy crude oil and bitumen.

[0072] Unlike MTG processes where gasoline is the end product, it is not necessary to remove heavier components like durene from the hydrocarbon stream when naphtha is the end product.

[0073] In some embodiments, the naphtha-based diluent has the following composition:
Table 2. Concentration of components in naphtha diluent.
Component Concentration (% vol) n-paraffin 12.5%
Iso-paraffin 29.2%
Cyclic paraffin 46.2%
Aromatics 12.1%

Date Recue/Date Received 2023-03-23

[0074] A typical distillation curve which is commonly used to describe a hydrocarbon product such as naphtha is shown in FIG. 5.

[0075] A byproduct of the naphtha synthesis is liquified petroleum gas (LPG) which is the light hydrocarbons Cl to C4 and which is removed to stabilize the naphtha. The LPG may be used as a fuel source in the subject methods 10, 30,40, for example for the reforming step 18.

[0076] System for Producing Naphtha from Captured CO2

[0077] FIG. 4 illustrates one embodiment of a system 60 suitable for carrying out the described methods. The system includes a reformer 42 that receives the feedstocks, which in the illustrated embodiment are captured CO2 12, H2 28, CH4 14 and H20 16.
Alternatively, the feedstocks may omit H228, or they may only include captured and H2 28. The reformer 42 reforms the feedstocks into syngas which is supplied to the methanol reactor 44 where methanol is synthesized. The methanol then enters the naphtha reactor 46 where naphtha is synthesized. The naphtha is fed into a distillation column 50 where it is separated into LPG 54 and naphtha (diluent) 56.

[0078] An energy source 52 provides energy to the reformer 42. The energy source may comprise the LPG 54 and/or an alternate energy source, such as natural gas or another fuel. H20 produced as a byproduct in the naphtha reactor 46 may be fed back into the H20 feedstock 16. CO2 produced in the methanol reactor 44 may be fed back into the captured CO2 feedstock.

[0079] In some embodiments, illustrated by the dashed lines in FIG. 4, the system 60 may include a DME reactor 48 which receives methanol from the methanol reactor 44, which is converted to DME and then fed into the naphtha reactor 46. Alternatively, the syngas from the reformer may go directly to the DME reactor 48 (not shown).

[0080] Although the present disclosure has been described and illustrated with respect to preferred embodiments and preferred uses thereof, it is not to be so limited since modifications and changes can be made therein which are within the full, intended scope of the disclosure as understood by those skilled in the art.

Date Recue/Date Received 2023-03-23

Claims (19)

1. A method for producing naphtha from captured carbon dioxide comprising the steps:
a) providing feedstocks including methane and captured carbon dioxide;
b) reforming the feedstocks to produce a synthesis gas comprising hydrogen, carbon monoxide and carbon dioxide;
c) synthesizing methanol from the synthesis gas; and d) synthesizing naphtha from the methanol.

2. The method of claim 1, wherein the feedstocks include hydrogen.

3. A method for producing naphtha from captured carbon dioxide comprising the steps:
a) providing feedstocks including hydrogen and captured carbon dioxide;
b) reforming the feedstocks to produce a synthesis gas comprising hydrogen, carbon monoxide and carbon dioxide;
c) synthesizing methanol from the synthesis gas; and d) synthesizing naphtha from the methanol.

4. The method of any one of claim 1-3, further comprising providing the naphtha as a diluent to reduce the viscosity of heavy crude oil or bitumen.

5. The method of any one of claims 1-4, wherein the synthesis gas comprises (H2 -CO2) / (CO + CO2) having a molar ratio of about 2.0 to about 2.1.

6. The method of any one of claims 1-5, wherein after step c), dimethyl ether is synthesized from the methanol, and the dimethyl ether is used to synthesize the naphtha.

Date Recue/Date Received 2023-03-23

7. The method of any one of claims 1-6, wherein the feedstocks include carbon dioxide captured from steam-assisted gravity drainage (SAGD) operations used in production of the heavy crude oil or bitumen.

8. The method of claim 1, wherein the reforming in step b) comprises steam methane reforming.

9. The method of claim 1, wherein the reforming in step b) comprises autothermal reforming.

10. The method of any one of claims 1-9, wherein synthesizing the naphtha includes removing light hydrocarbons C1 to C4.

11. The method of claim 1, wherein the feedstocks include natural gas.

12. The method of claim 1, wherein the feedstocks include biomethane.

13. The method of claim 2 or 3, wherein the feedstocks include hydrogen derived from biomass.

14. The method of claim 13, wherein the feedstocks include hydrogen derived from biomass gasification.

15. The method of claim 13, wherein the feedstocks include hydrogen derived from anaerobic digestion of biomass.

16. The method of claim 2 or 3, wherein the feedstocks include hydrogen derived from reforming of natural gas.

17. A system for producing naphtha from captured carbon dioxide comprising:
a source of methane;
a source of captured carbon dioxide;
a reformer for receiving the methane and captured carbon dioxide and producing synthesis gas;

Date Recue/Date Received 2023-03-23 a methanol reactor for synthesizing methanol from the synthesis gas;
a naphtha reactor for synthesizing naphtha from the methanol; and a fractionation or distillation unit for removing gaseous hydrocarbons from the naphtha.

18. The system of claim 17, further comprising a source of hydrogen for input into the reformer.

19. A system for producing naphtha from captured carbon dioxide comprising:
a source of hydrogen;
a source of captured carbon dioxide;
a reformer for receiving the hydrogen and captured carbon dioxide and producing synthesis gas;
a methanol reactor for synthesizing methanol from the synthesis gas;
a naphtha reactor for synthesizing naphtha from the methanol; and a fractionation or distillation unit for removing gaseous hydrocarbons from the naphtha.

Date Recue/Date Received 2023-03-23