Method and apparatus for producing hydrocarbons

Abstract

The present disclosure relates to a method and apparatus for producing hydrocarbons from organic waste. The method and apparatus for producing hydrocarbons, according to the present disclosure, can significantly improve the production yield of hydrocarbons from organic waste and expand the range of products that can be obtained from organic waste. In addition, the generation of carbon dioxide can be minimized during the hydrocarbon production process.

Description

Hydrocarbon production method and device

[0001] The present disclosure relates to a method and apparatus for producing hydrocarbons from carbon dioxide.

[0002] The excessive combustion of fossil fuels has led to a sharp increase in carbon dioxide (CO2) emissions, leading to a rapid increase in atmospheric CO2 concentrations. CO2 emissions from South Korea's industrial sector have been steadily increasing each year, reaching nearly 350 million tons in 2020. This increase in CO2 emissions has become a major contributor to global warming and other climate change.

[0003] With societal demands for carbon dioxide emissions reductions at an all-time high, companies, the main players in industry, are researching and developing carbon reduction measures. One such technology is Carbon Capture & Storage (CCS), a technology that captures and processes carbon dioxide emitted from smokestacks. This technology captures, transports, and stores carbon dioxide emitted from industrial processes in large quantities, allowing it to be utilized for improving the recovery of oil and natural gas. However, in Korea, it is difficult to find storage facilities, and considering the potential impact on the ecosystem and geological stability after storage, it is difficult to apply this technology.

[0004] Another technology is carbon capture and utilization (CCU). The large amounts of carbon dioxide generated from processes in various industries, including the petrochemical industry, can be utilized as a carbon source for the production of fuels and value-added chemicals in various carbon-based, eco-friendly technologies. Therefore, for the sustainable development and growth of various industries, carbon capture and utilization (CCU) technology is particularly crucial. It fundamentally reduces carbon dioxide emissions while simultaneously upcycling the emitted carbon dioxide to produce basic petrochemical products like ethylene.

[0005] Conventional methods for converting captured carbon dioxide into hydrocarbons typically involve hydrogenation using a copper catalyst to convert carbon dioxide into carbon monoxide and water, and then utilizing the carbon monoxide. However, this technology requires the use of large quantities of expensive hydrogen, necessitating the construction of both hydrogen production and high-purity hydrogen capture facilities, making it uneconomical.

[0006] Accordingly, there is a need for a hydrocarbon production method and production device that can efficiently produce high value-added hydrocarbons while reducing carbon dioxide by converting carbon dioxide into carbon monoxide at an excellent conversion rate using easy-to-handle raw materials.

[0007] The purpose of the present disclosure is to provide a method and apparatus for producing hydrocarbons using carbon dioxide captured from gas generated in the atmosphere or an external process.

[0008] In addition, another object of the present disclosure is to provide a method and apparatus for producing hydrocarbons using only raw materials that are easy to handle.

[0009] In addition, another object of the present disclosure is to provide a method and apparatus for producing hydrocarbons capable of converting carbon dioxide into carbon monoxide at an excellent conversion rate without by-products.

[0010] A method for producing hydrocarbons according to the present disclosure comprises: (S1) separating a first stream containing carbon dioxide from a feed gas; (S2) converting the carbon dioxide and an external carbon source contained in the first stream into a first mixed gas containing carbon monoxide by performing a reverse Boudouard reaction; (S3) converting a predetermined volume of the first mixed gas into a second mixed gas by performing a water gas shift reaction; (S4) separating the second mixed gas into a second stream containing carbon dioxide and a third stream containing hydrogen; and (S5) producing a hydrocarbon by performing a Fischer-Tropsch synthesis reaction on the remaining first mixed gas and the third stream that are not converted in the step (S3).

[0011] In one embodiment, steps (S1) and (S4) can be performed through the same carbon dioxide separation unit.

[0012] According to one embodiment, steps (S1) to (S5) are unit processes, and the unit processes can be repeated two or more times.

[0013] Before step (S3) according to one embodiment, a step of purifying the first mixed gas may be further included.

[0014] According to one embodiment, before the step (S5), a step of producing a third mixed gas by mixing the remaining first mixed gas not converted in the step (S3) and the third stream separated in the step (S4) may be further included.

[0015] The reverse reaction of step (S2) according to one embodiment can be performed at a temperature of 500 to 1000°C.

[0016] The water-to-gas shift reaction of step (S3) according to one embodiment can be performed at a temperature of 100 to 500° C. and a pressure of 10 to 50 bar.

[0017] The Fischer-Tropsch synthesis reaction of step (S5) according to one embodiment can be performed at a temperature of 150 to 500° C. and a pressure of 10 to 50 bar.

[0018] A hydrocarbon production device according to the present disclosure comprises: a first carbon dioxide separation unit for separating a first stream containing carbon dioxide from a feed gas; a reverse Buder reactor for converting carbon dioxide and an external carbon source contained in the first stream into a first mixed gas containing carbon monoxide; a water gas shift reactor for converting a predetermined volume of the first mixed gas into a second mixed gas; a second carbon dioxide separation unit for separating the second mixed gas into a second stream containing carbon dioxide and a third stream containing hydrogen; and a Fischer-Tropsch synthesis reactor for producing hydrocarbons by introducing the remaining first mixed gas not converted in the water gas shift reactor and the third stream separated by the second carbon dioxide separation unit.

[0019] According to one embodiment, the first carbon dioxide separation unit and the second carbon dioxide separation unit may be identical.

[0020] A hydrocarbon production device according to one embodiment may further include a purification unit for purifying the first mixed gas.

[0021] A hydrocarbon production device according to one embodiment may further include a mixing unit for mixing the remaining first mixed gas not converted in the water-to-gas shift reactor and the third stream separated by the second carbon dioxide separation unit.

[0022] The hydrocarbon production method and production device according to the present disclosure can produce high value-added hydrocarbons using carbon dioxide captured from gas generated in the atmosphere or an external process.

[0023] The hydrocarbon production method and production device according to the present disclosure are economical because they can convert carbon dioxide into carbon monoxide at an excellent conversion rate without by-products.

[0024] The hydrocarbon production method and production device according to the present disclosure can reduce the concentration of carbon dioxide in the atmosphere.

[0025] The hydrocarbon production method and production device according to the present disclosure require less equipment cost than conventional methods, thereby increasing the production of carbon dioxide-derived products.

[0026] Figure 1 is a schematic diagram showing a hydrocarbon production device according to the present disclosure.

[0027] Figure 2 is a schematic diagram showing a hydrocarbon production device when the same carbon dioxide separation unit is applied according to the present disclosure.

[0028] As used herein, the singular forms of terms may be construed to include the plural forms as well, unless otherwise specified.

[0029] The numerical ranges used herein include the lower and upper limits, all values ​​within those limits, all values ​​delimited by these limits, and all possible combinations of the upper and lower limits of numerical ranges defined in different ways. Unless otherwise specified herein, values ​​outside the numerical ranges that may arise due to experimental error or rounding of values ​​are also included in the defined numerical ranges.

[0030] The term "includes" as used herein is an open-ended description having the equivalent meaning of expressions such as "comprises," "contains," "has," and "characterizes," and does not exclude additional elements, materials, or processes not listed.

[0031] The unit of % used in this specification without special mention means weight % unless otherwise defined.

[0032] The 'carbon dioxide conversion rate' referred to in this specification may mean the molar ratio of carbon dioxide converted into carbon monoxide to carbon dioxide introduced into the process.

[0033] Conventionally, methods for converting carbon dioxide into hydrocarbons have typically involved hydrogenation using a copper catalyst to convert carbon dioxide into carbon monoxide and water, and then utilizing the converted carbon monoxide. However, this technology requires large quantities of expensive hydrogen, and thus requires hydrogen production and high-purity hydrogen capture facilities to apply the process, resulting in disadvantages in economic feasibility. Therefore, the inventors of the present disclosure have devised a method and device capable of producing high-value-added hydrocarbons with high efficiency and at a lower cost than conventional methods from carbon dioxide captured from the atmosphere or process gases. The hydrocarbon production method and device of the present disclosure will be described in detail below.

[0034] The present disclosure provides a method for producing hydrocarbons, comprising: (S1) separating a first stream containing carbon dioxide from a feed gas; (S2) converting the carbon dioxide and an external carbon source contained in the first stream into a first mixed gas containing carbon monoxide by performing a reverse Boudouard reaction; (S3) converting a predetermined volume of the first mixed gas into a second mixed gas by performing a water gas shift reaction; (S4) separating the second mixed gas into a second stream containing carbon dioxide and a third stream containing hydrogen and carbon monoxide; and (S5) performing a Fischer-Tropsch synthesis reaction on the remaining first mixed gas not converted in step (S3) and the third stream separated in step (S4) to produce a hydrocarbon.

[0035] The above step (S1) is a step of separating a first stream containing carbon dioxide from feed gas.

[0036] In one example, the separation of the first stream containing carbon dioxide from the feed gas in the step (S1) may be performed through a first carbon dioxide separation unit. In one example, the first carbon dioxide separation unit may be an amine scrubber. Typically, an amine scrubber binds and removes carbon dioxide through an amine-based material, and can separate components such as carbon dioxide and hydrogen sulfide from gas vapor and recover a gas containing hydrogen, carbon monoxide, or an inert gas. Therefore, the amine scrubber can separate carbon dioxide from the feed gas. Specifically, the amine scrubber can separate carbon dioxide from the feed gas through a reaction according to the following reaction scheme 1.

[0037] [Reaction Formula 1]

[0038] 2RNH2+ CO2↔ RNHCOO - + RNH3 +

[0039] As another example, the first carbon dioxide separation unit may be a CCS unit (Carbon capture and storage unit). When the CCS unit is used to separate carbon dioxide, the CCS unit may separate carbon dioxide from the feed gas using an adsorbent including one or more selected from calcium oxide, calcium hydroxide, dolomite, limestone, or trona.

[0040] In one example, the feed gas in step (S1) may be an exhaust gas generated from the atmosphere or an external process, but is not particularly limited as long as it contains carbon dioxide. Meanwhile, the external process may refer to any process capable of generating carbon dioxide in various industrial fields.

[0041] The above step (S2) is a step of converting the carbon dioxide and external carbon source contained in the first stream separated in the above step (S1) into a first mixed gas containing carbon monoxide by performing a reverse Boudouard reaction. The reverse Boudouard reaction may be accompanied by the following reaction formula 2.

[0042] [Reaction Formula 2]

[0043] C+CO2→ 2CO

[0044] In one example, the external carbon source may be one or more selected from the group consisting of, but not limited to, graphite, pyrolysis char, bio char, and activated carbon.

[0045] In one example, the reverse reaction of step (S2) may be performed at a temperature of 600 to 1000°C, specifically 650 to 900°C, more specifically 700 to 800°C, and may be performed at a pressure of 0.5 to 30 bar, specifically 1 to 15 bar, more specifically 2 to 5 bar, but is not limited thereto.

[0046] In one example, the reverse reaction of step (S2) can be performed in a fixed-bed reactor. When this is satisfied, carbon dioxide can be converted into carbon monoxide with high efficiency even if the first stream contains low-purity carbon dioxide. However, this is not a limitation as long as the purpose of the present disclosure can be achieved.

[0047] In one example, the hydrocarbon production method of the present disclosure may further include a step of purifying the first mixed gas. The first mixed gas may include, in addition to carbon monoxide, one or more impurities selected from the group consisting of tar, sulfur, nitrogen, chlorine, and heavy metals. Specifically, the first mixed gas may include water-soluble impurities such as H2S, HCl, COS, HOCl, and NH3, and insoluble impurities such as tar and heavy metals. Such impurities included in the first mixed gas may induce deactivation of the catalyst used in the present disclosure, thereby reducing the efficiency of the subsequent process. Therefore, the step of purifying the first mixed gas can remove impurities, thereby improving the efficiency of the overall process.

[0048] In one example, the step of purifying the first mixed gas may be performed through one or a combination of two or more selected from the group consisting of passing through a high-pressure dust filter, water washing, alkaline solution washing, and passing through a ceramic filter, but is not limited thereto. When water washing or alkaline solution washing is used, water-soluble impurities such as H2S, HCl, COS, HOCl, and NH3 contained in the first mixed gas can be removed, and when the first mixed gas is passed through a ceramic filter or a dust filter, insoluble impurities such as tar and heavy metals and dust can be removed.

[0049] The above step (S3) is a step of converting a predetermined volume of the first mixed gas into a second mixed gas by a water gas shift reaction. Through the water gas shift reaction, the hydrogen:carbon monoxide ratio in the first mixed gas is adjusted, so that the subsequent Fischer-Tropsch synthesis reaction can be easily performed. Specifically, the water gas shift reaction may be a step in which carbon monoxide and water contained in the first mixed gas react as in the following reaction formula 3 to convert them into a second mixed gas.

[0050] [Reaction Formula 3]

[0051] CO + H2O → H2 + CO2

[0052] In one example, the predetermined volume may be, based on the total volume of the first mixed gas, a lower limit of 10% by volume or more, 20% by volume or more, 30% by volume or more, 40% by volume or more, or 45% by volume or more, and an upper limit of 100% by volume or less, 80% by volume or less, 70% by volume or less, 60% by volume or less, or 55% by volume or less, and specifically, may be, but is not limited to, 10 to 90% by volume, 20 to 80% by volume, 30 to 70% by volume, 40 to 60% by volume, or 45 to 55% by volume.

[0053] In one example, the water-gas shift reaction can be performed under a water-gas shift catalyst comprising Cu, Zn or a combination thereof, and as a specific example, it can be performed under a water-gas shift catalyst in which Cu and Zn are supported on an alumina support, but is not limited thereto.

[0054] In one example, the water-gas shift reaction can be performed at a temperature of 100 to 500°C, specifically 125 to 300°C, more specifically 150 to 200°C, and a pressure of 20 to 80 bar, specifically 25 to 60 bar, more specifically 30 to 40 bar.

[0055] In one example, the second mixed gas may include hydrogen and carbon dioxide.

[0056] The above step (S4) is a step of separating the second mixed gas into a second stream containing carbon dioxide and a third stream containing hydrogen.

[0057] In one example, in step (S4), separating the second mixed gas into a second stream containing carbon dioxide and a third stream containing hydrogen may be performed through a second carbon dioxide separation unit. The description of the first carbon dioxide separation unit described above may be equally applied to the description of the second carbon dioxide separation unit to the extent that there is overlap.

[0058] In one example, step (S4) may be performed using the same carbon dioxide separation unit as step (S1). In this case, the carbon dioxide generated in step (S3) is not only not released into the atmosphere, but can also be recycled to participate in the reverse reaction of step (S2), thereby significantly increasing the carbon dioxide conversion rate and securing economic feasibility.

[0059] In one example, when the step (S4) is performed through the same first carbon dioxide separation unit as the step (S1), the hydrocarbon production method of the present disclosure may comprise steps (S1) to (S5) as a unit process, and repeat the unit process two or more times. By repeating the unit process two or more times to continuously convert carbon dioxide into hydrocarbons, the carbon dioxide conversion rate can be significantly increased. Meanwhile, when the hydrocarbon production method of the present disclosure further comprises an additional step in addition to steps (S1) to (S5), the unit process may of course include the additional step.

[0060] The above step (S5) is a step of producing hydrocarbons by subjecting the remaining first mixed gas that was not converted in the above step (S3) and the third stream separated in the above step (S4) to a Fischer-Tropsch synthesis reaction. Specifically, carbon monoxide and hydrogen contained in the first mixed gas and hydrogen contained in the third stream may be mixed and then reacted to produce hydrocarbons. The Fischer-Tropsch synthesis reaction may be accompanied by the following reaction scheme 4.

[0061] [Reaction Formula 4]

[0062] nCO + 2nH2→C n H 2n + nH2O

[0063] In one example, the Fischer-Tropsch synthesis reaction of the above step (S5) can be performed under a Fischer-Tropsch reaction catalyst including cobalt, nickel or iron, and can include alumina, silica, titania, etc. as a support, and can include a noble metal such as Pt, Ru, Re, etc. as a cocatalyst.

[0064] In one example, the Fischer-Tropsch synthesis reaction of step (S5) may be performed at a temperature of 100 to 500°C, specifically 200 to 350°C, and at a pressure of 10 to 50 bar, specifically 20 to 40 bar. When the above ranges are satisfied, the yield of the produced hydrocarbon is excellent.

[0065] In one example, the hydrocarbon production method according to the present disclosure may further include, before step (S5), a step of producing a third mixed gas by mixing the third stream separated in the second carbon dioxide separation unit with the remaining first mixed gas that was not converted in step (S3). In this case, a single stream including the third mixed gas may be fed into a Fischer-Tropsch synthesis reactor to cause a Fischer-Tropsch synthesis reaction.

[0066] In one example, the third mixed gas has a molar ratio of hydrogen and carbon monoxide (m H2 / m CO ) may be 1 to 10, specifically 1.3 to 5, and more specifically 1.8 to 2.5. When the above range is satisfied, the efficiency of the Fischer-Tropsch synthesis reaction may be increased.

[0067] In one example, the hydrocarbon production method of the present disclosure may further include a separation step for separating the hydrocarbon produced in step (S5). In one example, the method for separating the hydrocarbon produced in step (S5) is not particularly limited as long as it is a method known in the art, but may be distillation as an example.

[0068] In another aspect, the present disclosure provides a hydrocarbon production apparatus, comprising: a first carbon dioxide separation unit for separating a first stream containing carbon dioxide from a feed gas; a reverse Buder reactor for converting carbon dioxide and an external carbon source contained in the first stream into a first mixed gas containing carbon monoxide; a water gas shift reactor for converting a predetermined volume of the first mixed gas into a second mixed gas; a second carbon dioxide separation unit for separating the second mixed gas into a second stream containing carbon dioxide and a third stream containing hydrogen; and a Fischer-Tropsch synthesis reactor for producing hydrocarbons by introducing the remaining first mixed gas not converted in the water gas shift reactor and the third stream separated by the second carbon dioxide separation unit. The hydrocarbon production apparatus according to the present disclosure can efficiently and economically produce hydrocarbons by including the above configuration, and can significantly reduce carbon dioxide emissions.

[0069] The description of the hydrocarbon production method may be equally applied to the description of the hydrocarbon production device to the extent of overlap.

[0070] Referring to FIG. 1, after the feed gas (100) is introduced into the first carbon dioxide separation unit (10), a first stream (120) containing carbon dioxide can be separated from the feed gas (100). The first stream (120) separated by the first carbon dioxide separation unit (10) and an external carbon source (130) can be introduced into the reverse catalytic reactor (20) and converted into a first mixed gas (140) containing carbon monoxide.

[0071] In one example, the hydrocarbon production device of the present disclosure may further include a purification unit (25). The purification unit may be positioned between the reverse Buda reactor (20) and the water-to-gas shift reactor (30) to remove impurities from the first mixed gas (140) converted from the reverse Buda reactor (20) and to introduce the first mixed gas (150, 160) from which the impurities have been removed into the water-to-gas shift reactor (30). Specifically, the purification unit (25) may include a sprayer that sprays a liquid to receive the first mixed gas (140) from the reverse Buda reactor (20) and to contact the first mixed gas (140) with a weakly basic solution containing a basic compound such as water or sodium carbonate to remove water-soluble impurities such as H2S, HCl, COS, HOCl, and NH3. Additionally, dust can be removed using a high-pressure dust collection filter, and insoluble impurities such as tar and heavy metals can be removed using a ceramic filter, etc.

[0072] In one example, the purification unit may include a plurality of units (25-1, 25-2), and specifically, the plurality of units may include a scrubber and an adsorption bed. When this is satisfied, water-soluble and water-insoluble impurities can be removed in stages, thereby improving purification efficiency.

[0073] A predetermined volume of the first mixed gas (150, 160) and water (180) can be introduced into the water gas conversion reactor (30) by a stream separating device and converted into a second mixed gas (190) containing hydrogen and carbon dioxide.

[0074] The second carbon dioxide separation unit (40) can separate the second mixed gas (190) into a second stream (200) containing carbon dioxide and a third stream (210) containing hydrogen. If the hydrocarbon production device of the present disclosure further includes the purification unit, it is of course possible to separate the second mixed gas from which the impurities have been removed.

[0075] Referring to FIGS. 1 and 2, in one example, the first carbon dioxide separation unit (10) and the second carbon dioxide separation unit (40) may be the same. In this case, the carbon dioxide separated from the second mixed gas (190) may not be discharged into the atmosphere, but may be recycled to significantly increase the carbon dioxide conversion rate. In addition, the process may be operated with a single carbon dioxide separation unit, thereby ensuring economic feasibility.

[0076] The remaining first mixed gas (170) that is not converted in the above-mentioned water-to-gas shift reactor (30) and the third stream (210) separated by the second carbon dioxide separation unit (40) are introduced into the above-mentioned Fischer-Tropsch synthesis reactor (50) and converted into hydrocarbons (230) through the Fischer-Tropsch synthesis reaction, which can be recovered as a high value-added oil fraction.

[0077] In one example, the hydrocarbon production device of the present disclosure may further include a mixing unit (45) that mixes the remaining first mixed gas (170) not converted in the water-to-gas shift reactor (30) and the third stream (210) separated by the second carbon dioxide separation unit (40) to produce a third mixed gas (220). In this case, the third mixed gas (220) may be supplied to the Fischer-Tropsch synthesis reactor (50) and converted into hydrocarbons.

[0078] In one example, the hydrocarbon production device of the present disclosure may further include a separation unit (not shown) for separating hydrocarbons produced in the Fischer-Tropsch synthesis reactor. In one example, the separation unit may be, but is not limited to, a distillation column.

[0079] The following examples further illustrate the hydrocarbon production method and apparatus according to the present disclosure. However, the following examples are merely a reference for further illustrating the present disclosure and are not intended to limit the present disclosure, which may be implemented in various forms. Furthermore, 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 to which this disclosure pertains. Furthermore, the terminology used in the description of this disclosure is solely for the purpose of effectively describing specific embodiments and is not intended to limit the present disclosure.

[0080] Gas composition analysis method

[0081] Gas composition analysis was performed using gas chromatography (GC), and the total gas amount was confirmed using a gas meter. Specifically, the gas selectivity was calculated by quantifying the gas through GC, and the composition of each gas was analyzed using the total gas amount confirmed by the gas meter.

[0082] Example

[0083] 1. Carbon dioxide separation

[0084] Feed gas generated from a coal gasification process was fed into the first Amine Scrubber, and carbon dioxide was captured under the conditions of 50°C, 15 bar, and 12 wt% ammonia aqueous solution. Then, the ammonia aqueous solution with carbon dioxide captured was fed into the second Amine Scrubber, separated into ammonia aqueous solution and carbon dioxide at 100°C, and the carbon dioxide was recovered as the first stream.

[0085] 2. Reverse Buddha reaction

[0086] The recovered first stream was continuously supplied to a fixed bed reactor filled with 5 kg of Ni / Al2O3 catalyst and high-purity graphite, and the first mixed gas containing carbon monoxide was captured by converting carbon dioxide into carbon monoxide through the reverse Buta reaction, and the composition of the main components is shown in Table 1 below. The reverse Buta reaction was performed under N2 gas at 750°C, CO2 flow rate of 2.33 Nl / min, and space velocity of 2.0 L / g. cat ·It was performed for 2 hours under the condition of h.

[0087] Before Gas Reaction (vol%) After Reaction (vol%) Main Components (vol%) H2N / DN / DCH4N / DN / DCO210014.7CON / D85.3

[0088] (N / D: Not Detected, not detected.)

[0089] 3. Water-gas shift reaction

[0090] After the first mixed gas is sequentially passed through an adsorption tower and a scrubber composed of calcium oxide, 66.7% of the purified first mixed gas and purified water are introduced into a water gas conversion unit and, under the Cu / Zn / Al2O3 catalyst, 165 o C, 35 bar, space velocity 1.4 L / g cat·The water-gas shift reaction is performed under h conditions to convert into a second mixed gas containing carbon dioxide and hydrogen, and the composition of the main components is shown in Table 2 below.

[0091] Main component Before WGS reaction (mol) After WGS reaction (mol) Main component (mol) H2N / D56.9CO214.771.6CO85.328.4

[0092] 4. Separation of carbon dioxide and hydrogen

[0093] The above second mixed gas was fed into the first Amine Scrubber, and carbon dioxide was captured under the same conditions as when carbon dioxide was captured from the feed gas. Then, the ammonia aqueous solution containing carbon dioxide was introduced into the second Amine Scrubber and separated into the ammonia aqueous solution and carbon dioxide at 100°C, thereby recovering streams containing carbon dioxide and hydrogen, respectively.

[0094] 5. Gas mixing

[0095] The remaining first mixed gas not used in the water-gas shift reaction and the stream containing hydrogen separated from the second mixed gas were introduced into a gas mixing unit and mixed at 200°C to produce a third mixed gas.

[0096] 6. Fischer-Tropsch synthesis reaction

[0097] The above third mixed gas is supplied to the Fischer-Tropsch synthesis reactor and is produced under the Co(10%) / ZrO2 catalyst at a space velocity of 1.6 L / g. cat ·h, 245 ℃, 35 bar Fischer-Tropsch synthesis reaction was performed to recover hydrocarbons, and the composition of the main components is shown in Table 3 below.

[0098] Main component selectivity (%) Main component (mol) Gas 38.7 Liquid, Wax 25.5 H2O 35.8

[0099] As shown in Tables 1 through 3, the hydrocarbon production method according to the examples safely converts carbon dioxide into hydrocarbons using only readily available carbon and water, without the need for high-purity hydrogen. Furthermore, carbon dioxide is converted to carbon monoxide at a high conversion rate without byproducts. Considering recycling, a carbon dioxide conversion rate of approximately 100% can be achieved, ensuring economic feasibility.

[0100] Although the present disclosure has been described with specific details and limited examples, these are provided only to help a more general understanding of the present disclosure, and the present disclosure is not limited to the above examples, and those skilled in the art to which the present disclosure pertains can make various modifications and variations based on these descriptions.

[0101] Therefore, the spirit of the present disclosure should not be limited to the described embodiments, and all things that are equivalent or equivalent to the following claims as well as the claims are considered to fall within the scope of the spirit of the present disclosure.

[0102] [Explanation of symbols]

[0103] 10. 1st carbon dioxide separation unit

[0104] 20 Reverse Buddha Reactor

[0105] 25-1, 25-2 Refining Unit

[0106] 30 Water-Gas Shift Reactor

[0107] 40 Second Carbon Dioxide Separation Unit

[0108] 45 mixed units

[0109] 50 Fischer-Tropsch synthesis reactors

[0110] 100 feed gas

[0111] 110 Carbon dioxide separated feed gas

[0112] 120 1st stream

[0113] 130 External carbon sources

[0114] 140 First mixed gas

[0115] 150, 160 purified first mixed gas

[0116] 170 Remaining first mixed gas

[0117] 180 water

[0118] 190 Second mixed gas

[0119] 200 Second Stream

[0120] 210 Third Stream

[0121] 220 Third mixed gas

[0122] 230 hydrocarbons

Claims

1. (S1) A step of separating a first stream containing carbon dioxide from a feed gas; (S2) A step of converting the carbon dioxide and external carbon source included in the first stream into a first mixed gas containing carbon monoxide by performing a reverse Boudouard reaction; (S3) A step of converting a predetermined volume of the first mixed gas into a second mixed gas by performing a water gas shift reaction; (S4) a step of separating the second mixed gas into a second stream containing carbon dioxide and a third stream containing hydrogen; and (S5) A method for producing hydrocarbons, comprising: a step of producing hydrocarbons by subjecting the remaining first mixed gas and the third stream that were not converted in the step (S3) to a Fischer-Tropsch synthesis reaction.

2. In paragraph 1, A method for producing hydrocarbons, wherein the above steps (S1) and (S4) are performed through the same carbon dioxide separation unit.

3. In paragraph 2, A method for producing hydrocarbons, wherein the above steps (S1) to (S5) are repeated as unit processes at least twice.

4. In paragraph 1, A method for producing hydrocarbons, further comprising a step of purifying the first mixed gas before the step (S3).

5. In paragraph 1, A method for producing hydrocarbons, further comprising, before the step (S5), a step of producing a third mixed gas by mixing the remaining first mixed gas not converted in the step (S3) and the third stream separated in the step (S4).

6. In paragraph 1, A method for producing hydrocarbons, wherein the reverse reaction of the above step (S2) is performed at a temperature of 500 to 1000°C.

7. In paragraph 1, A method for producing hydrocarbons, wherein the water-to-gas shift reaction of the above step (S3) is performed at a temperature of 100 to 500°C and a pressure of 10 to 50 bar.

8. In paragraph 1, A method for producing hydrocarbons, wherein the Fischer-Tropsch synthesis reaction of the above step (S5) is performed at a temperature of 150 to 500°C and a pressure of 10 to 50 bar.

9. A first carbon dioxide separation unit for separating a first stream containing carbon dioxide from a feed gas; A reverse carburetor reactor for converting carbon dioxide and an external carbon source contained in the first stream into a first mixed gas containing carbon monoxide; A water-gas shift reactor that converts a predetermined volume of the first mixed gas into a second mixed gas; A second carbon dioxide separation unit that separates the second mixed gas into a second stream containing carbon dioxide and a third stream containing hydrogen; and A hydrocarbon production device comprising a Fischer-Tropsch synthesis reactor that produces hydrocarbons by injecting the remaining first mixed gas not converted in the water gas shift reactor and the third stream separated by the second carbon dioxide separation unit.

10. In paragraph 9, A hydrocarbon production device wherein the first carbon dioxide separation unit and the second carbon dioxide separation unit are the same.

11. In paragraph 9, A hydrocarbon production device further comprising a purification unit for purifying the first mixed gas.

12. In paragraph 9, A hydrocarbon production device further comprising a mixing unit for mixing the remaining first mixed gas not converted in the water-to-gas shift reactor and the third stream separated by the second carbon dioxide separation unit.

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