WO2022264836A1 - 炭化水素製造装置および炭化水素製造方法 - Google Patents
炭化水素製造装置および炭化水素製造方法 Download PDFInfo
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- WO2022264836A1 WO2022264836A1 PCT/JP2022/022612 JP2022022612W WO2022264836A1 WO 2022264836 A1 WO2022264836 A1 WO 2022264836A1 JP 2022022612 W JP2022022612 W JP 2022022612W WO 2022264836 A1 WO2022264836 A1 WO 2022264836A1
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- hydrogen
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- hydrocarbon production
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- C—CHEMISTRY; METALLURGY
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/40—Carbon monoxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/12—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon dioxide with hydrogen
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
- C07C31/04—Methanol
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
- C07C9/04—Methane
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/14—Aliphatic saturated hydrocarbons with five to fifteen carbon atoms
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/026—Increasing the carbon monoxide content, e.g. reverse water-gas shift [RWGS]
Definitions
- the present invention relates to a hydrocarbon production device and a hydrocarbon production method.
- a technology for producing liquid fuel by GTL (Gas to Liquid) is known (see Patent Document 1).
- FT reaction a Fischer-Tropsch reaction
- FT reaction a Fischer-Tropsch reaction
- the present invention has been made in view of this situation, and one of its purposes is to provide a technique for improving the efficiency of hydrocarbon production.
- One aspect of the present invention is a hydrocarbon production device.
- This apparatus uses carbon dioxide and hydrogen as source gases and reduces the carbon dioxide to carbon monoxide by a reverse shift reaction to obtain a synthesis gas containing carbon monoxide and hydrogen; and a gaseous component containing hydrogen, carbon dioxide and light hydrocarbons having 4 or less carbon atoms, and hydrocarbons having 5 or more carbon atoms from the effluent from the hydrocarbon manufacturing portion.
- a gas-liquid separation unit that separates the liquid component containing, a first separation unit that separates hydrogen, carbon dioxide, and light hydrocarbons from the gas component, and supply of the light hydrocarbons separated by the first separation unit and a catalytic reaction section for receiving and using the light hydrocarbons to produce hydrogen and carbon monoxide.
- the reverse shift reaction section receives the supply of hydrogen and carbon dioxide separated by the first separation section, and also uses the hydrogen and carbon dioxide to generate synthesis gas.
- the hydrocarbon production section receives the supply of hydrogen and carbon monoxide produced by the catalytic reaction section, and uses the hydrogen and carbon monoxide to produce hydrocarbons.
- Another aspect of the present invention is a hydrocarbon production method.
- This method includes a reverse shift reaction step of using carbon dioxide and hydrogen as source gases and reducing the carbon dioxide to carbon monoxide by a reverse shift reaction to obtain a synthesis gas containing carbon monoxide and hydrogen; and a gaseous component containing hydrogen, carbon dioxide and light hydrocarbons having 4 or less carbon atoms, and hydrocarbons having 5 or more carbon atoms from the effluent from the hydrocarbon manufacturing process.
- a gas-liquid separation step of separating the liquid component containing the liquid component a first separation step of separating hydrogen and carbon dioxide, and light hydrocarbons from the gas component, and supply of the light hydrocarbons separated in the first separation step and a catalytic reaction step for producing hydrogen and carbon monoxide using the light hydrocarbons.
- the reverse shift reaction step the hydrogen and carbon dioxide separated in the first separation step are supplied, and the hydrogen and carbon dioxide are also used to generate synthesis gas.
- hydrogen and carbon monoxide produced in the catalytic reaction step are supplied, and the hydrogen and carbon monoxide are also used to produce hydrocarbons.
- FIG. 1 is a schematic diagram of a hydrocarbon production apparatus according to an embodiment
- FIG. FIG. 3 is a schematic diagram of a hydrocarbon production apparatus according to a comparative example
- 1 is a schematic diagram of a hydrocarbon production apparatus according to Test Example 1.
- FIG. 2 is a schematic diagram of a hydrocarbon production apparatus according to Test Example 2.
- FIG. 2 is a schematic diagram of a hydrocarbon production apparatus according to Test Example 3.
- FIG. FIG. 10 is a schematic diagram of a hydrocarbon production apparatus according to Test Example 4;
- FIG. 1 is a schematic diagram of a hydrocarbon production device 1 according to an embodiment.
- the hydrocarbon production apparatus 1 includes a reverse shift reaction section 2, a hydrocarbon production section 4, a gas-liquid separation section 6, a contact reaction section 8, a first separation section 10, a second separation section 12, and a third It has a separation section 14 , a fourth separation section 16 and a fifth separation section 18 .
- the reverse shift reaction section 2 is arranged upstream of the hydrocarbon production section 4 .
- a fourth separation section 16 is arranged between the reverse shift reaction section 2 and the hydrocarbon production section 4 .
- a gas-liquid separation unit 6 is arranged downstream of the hydrocarbon production unit 4 .
- a first separation section 10 is arranged between the gas-liquid separation section 6 and the reverse shift reaction section 2 and the contact reaction section 8 .
- a second separation section 12 is arranged in parallel with the first separation section 10 between the gas-liquid separation section 6 and the contact reaction section 8 .
- a third separation section 14 is arranged between the second separation section 12 and the contact reaction section 8 .
- a fifth separation section 18 is arranged between the contact reaction section 8 and the hydrocarbon production section 4 .
- the reverse shift reaction section 2 is supplied with carbon dioxide and hydrogen as source gases. Carbon dioxide and hydrogen are then used to reduce the carbon dioxide to carbon monoxide by a reverse shift reaction to obtain synthesis gas containing carbon monoxide and unreacted hydrogen.
- the reverse shift reaction section 2 of the present embodiment receives supply of hydrogen from the water electrolysis module 20 as an example.
- the water electrolysis module 20 is illustrated as an external device with respect to the hydrocarbon production apparatus 1 in FIG. 1 , the water electrolysis module 20 may be incorporated inside the hydrocarbon production apparatus 1 .
- the water electrolysis module 20 is an electrolytic cell that generates hydrogen and oxygen by electrolyzing water.
- the water electrolysis module 20 has a structure in which an oxygen generating electrode having a catalyst such as iridium or platinum and a hydrogen generating electrode having a catalyst such as platinum are separated by a diaphragm having proton conductivity. That is, the water electrolysis module 20 is a polymer electrolyte water electrolysis module.
- Other examples of the water electrolysis module 20 include an alkaline water electrolysis module and a solid oxide water electrolysis module.
- the reactions during electrolysis of water in the polymer electrolyte water electrolysis module are as shown in the following formulas (1) and (2). Reaction Occurring at the Oxygen Evolving Electrode: 2H 2 O ⁇ O 2 +4H + +4e ⁇ (1) Reaction occurring at hydrogen evolution electrode: 4H + +4e ⁇ ⁇ 2H 2 (2)
- the water electrolysis module 20 receives power necessary for water electrolysis from a power supply device (not shown).
- power supply devices include power generation devices that generate power using renewable energy, such as wind power generation devices and solar power generation devices. As a result, it is possible to reduce the amount of carbon dioxide emissions associated with the production of hydrogen and the production of target hydrocarbons having 5 or more carbon atoms (hereinafter referred to as "C5+ components" as appropriate).
- the power supply device is not limited to a power generation device that uses renewable energy, and may be a grid power source, a renewable energy power generation device, or a power storage device that stores power from a grid power source. good. Also, a combination of two or more of these may be used.
- the power supply device is preferably a power generation device that uses renewable energy.
- the amount of carbon dioxide emissions associated with power generation and power storage is preferably equal to or less than that of a power generation device that uses renewable energy.
- the reverse shift reaction section 2 of the present embodiment receives supply of carbon dioxide from the carbon dioxide recovery section 22 as an example.
- FIG. 1 shows the carbon dioxide recovery unit 22 as an external device to the hydrocarbon production apparatus 1
- the carbon dioxide recovery unit 22 may be incorporated inside the hydrocarbon production apparatus 1 .
- the hydrocarbon production apparatus 1 does not mean that the whole is one reactor.
- the carbon dioxide recovery unit 22 can recover carbon dioxide from the atmosphere, for example, by direct air recovery (DAC) or the like. Further, the carbon dioxide recovery unit 22 can separate and recover carbon dioxide from the exhaust gas discharged from a thermal power plant, a chemical plant, or the like by a chemical adsorption method or the like. By supplying carbon dioxide to the reverse shift reaction section 2 from the carbon dioxide recovery section 22, reduction of carbon dioxide in the atmosphere and exhaust gas can be expected. Also, the consumption of fossil fuels associated with the production of C5+ components can be reduced.
- DAC direct air recovery
- a reverse shift reaction represented by the following formula (3) occurs, and carbon dioxide is reduced to carbon monoxide.
- synthesis gas containing at least carbon monoxide and unreacted hydrogen is obtained.
- the synthesis gas also contains water produced by the reverse shift reaction. Syngas may also contain unreacted carbon dioxide. H2+ CO2 ⁇ CO + H2O (3)
- the reaction temperature in the reverse shift reaction section 2 is, for example, 290°C or higher and 1100°C or lower, preferably 700°C or higher and 1100°C or lower, and more preferably 700°C or higher and 950°C or lower.
- the reverse reaction of equation (3) is called the water gas shift reaction.
- a catalyst for the water-gas shift reaction may be used as the catalyst for the reverse shift reaction.
- reaction temperatures above 700° C. are much higher than temperatures in typical water gas shift reactions. For this reason, when setting the reaction temperature to a high temperature of 700° C. or higher, a general water gas shift catalyst is not suitable for use.
- the reverse shift reaction section 2 of the present embodiment contains a composite oxide having a perovskite structure ABO 3 as a reverse shift catalyst.
- A is an alkaline earth metal selected from the group consisting of calcium (Ca), strontium (Sr), barium (Ba), preferably barium.
- B is a metal selected from the group consisting of titanium (Ti), aluminum (Al), zirconium (Zr), iron (Fe), tungsten (W), molybdenum (Mo), preferably zirconium.
- B is titanium or zirconium, it may be partially substituted with manganese (Mn), iron (Fe) or cobalt (Co), preferably partially substituted with manganese.
- the reverse shift catalyst preferably does not have acid sites that break bonds between carbon atoms of hydrocarbons, and does not have hydrogen dissociation ability that breaks bonds between hydrogen atoms of hydrogen.
- the reverse shift catalyst having this feature for example, in a catalytic reaction using a mixed gas consisting of isobutene and hydrogen, it is confirmed that hydrocarbons with 8 carbon atoms due to dimerization and isobutane due to hydrogenation are not produced. can be screened.
- the reverse shift reaction can be realized while suppressing side reactions such as methanation at a high temperature of 700° C. or higher.
- an atomic absorption spectrophotometer it is preferable to use an atomic absorption spectrophotometer, a Fourier transform infrared spectrophotometer, or the like to measure whether the raw material gas for the reverse shift reaction contains any metal components.
- a filter capable of removing fine powder of metal carbide generated by carburization and an adsorbent capable of removing metal carbonyl on the recycling line through which carbon monoxide flows.
- the filter is preferably made of ceramic and the adsorbent is preferably Y-type zeolite.
- a carbon dioxide removal device is provided between the reverse shift reaction section 2 and the hydrocarbon production section 4 in order to reduce the carbon dioxide concentration in the synthesis gas.
- a carbon dioxide removal device is provided between the reverse shift reaction section 2 and the hydrocarbon production section 4 in order to reduce the carbon dioxide concentration in the synthesis gas. may be installed.
- the CO/(CO+CO 2 ) ratio is a value calculated from the carbon monoxide concentration and the carbon dioxide concentration at the outlet of the reverse shift reaction section 2 . That is, it is the rate at which the raw material carbon dioxide is converted (reduced) to carbon monoxide. Therefore, the carbon dioxide concentration at the outlet of the reverse shift reaction section 2 can be reduced.
- the partial pressure of the synthesis gas composed of carbon monoxide and hydrogen in the hydrocarbon production section 4 can be increased, and the carbon monoxide conversion rate and the selectivity of C5+ components can be improved.
- the thermal energy required for the carbon dioxide removal device can be supplied from the hydrocarbon production section 4 that utilizes the FT reaction, which is an exothermic reaction. As a result, the energy required for hydrocarbon production can be reduced, and the production efficiency of the target C5+ component can be improved.
- the reverse shift reaction by performing the reverse shift reaction at a high temperature of 700°C or higher, it is possible to suppress the generation of oxygenated hydrocarbons and the like. As a result, it is possible to prevent oxygenated hydrocarbons, which are impurities, from being contained in the by-product water. Therefore, the water separated in the fourth separation section 16 located downstream of the reverse shift reaction section 2 can be recycled to the water electrolysis module 20 without purification treatment (removal of oxygen-containing impurities). When the high-temperature reverse shift reaction is not performed, the water separated by the fourth separation unit 16 can be supplied to the third separation unit 14, which will be described later, so that the water can be purified.
- the off-gas from the hydrocarbon production section 4 is recycled to improve the production efficiency of the C5+ component, but this recycling also requires energy.
- the improved CO/(CO+CO 2 ) ratio increases the yield of liquid components, thereby reducing the amount of recycled off-gas. Therefore, it is possible to reduce auxiliary power required for recycling, energy required for separation of off-gas, amount of heat required for contact reaction at the recycling destination, and the like. As a result, an improvement in the production efficiency of the entire C5+ component production process can be expected.
- the synthesis gas flowing out of the reverse shift reaction section 2 is sent to the fourth separation section 16 .
- the fourth separation section 16 can be composed of a known gas-liquid separator and separates water from the synthesis gas.
- the water separated by the fourth separation unit 16 is supplied to the water electrolysis module 20 and used to generate hydrogen. Further, the water separated by the fourth separation section 16 is supplied to the contact reaction section 8 and used for the contact reaction in the contact reaction section 8 .
- recycling of the water separated from the synthesis gas may be performed for only one of the water electrolysis module 20 and the contact reaction section 8, or may not be performed for both.
- the synthesis gas from which water has been separated in the fourth separation section 16 is sent to the hydrocarbon production section 4 .
- the hydrocarbon production unit 4 produces the target C5+ component using the supplied synthesis gas.
- C5+ components are, for example, normal paraffins.
- the hydrocarbon production section 4 of the present embodiment is composed of a known FT reactor.
- a tubular fixed bed reactor, a slurry bed reactor, or the like can be used.
- the FT reaction represented by the formula (4) below occurs, and the C5+ component is produced by carbon-carbon chain growth.
- a cobalt catalyst, a precipitated iron catalyst, a ruthenium catalyst, or the like can be used as a catalyst for the FT reaction.
- the rate at which a reaction intermediate having n carbon atoms is heavier to a reaction intermediate having n+1 carbon atoms through carbon-carbon chain growth is expressed by the chain growth probability ⁇ .
- ⁇ varies depending on the type of catalyst and reaction conditions, and is preferably 0.75 to 0.95, more preferably 0.85 to 0.95.
- n of the C5+ component contained at 0.1 mol % or more is an integer of 5-60.
- light hydrocarbons such as methane, ethane, propane, and butane which are gaseous at normal temperature and pressure and have 4 or less carbon atoms (hereinafter referred to as “C4-component”) are also produced as by-products.
- C4-component light hydrocarbons such as methane, ethane, propane, and butane which are gaseous at normal temperature and pressure and have 4 or less carbon atoms
- the effluent from hydrocarbon production section 4 is sent to gas-liquid separation section 6 .
- This effluent contains not only C5+ and C4- components, but also other by-products such as water and oxygenated hydrocarbons (such as CnHmO ), as well as unreacted hydrogen, carbon monoxide and carbon dioxide. can be included.
- Oxygenated hydrocarbons are hydrocarbon compounds containing oxygen, which are hydrophilic and readily soluble in water. Examples of oxygenated hydrocarbons include alcohols, carboxylic acids, esters, ethers, ketones, and the like.
- the gas-liquid separator 6 can be composed of a known gas-liquid separator, and separates the liquid component and the gas component from the effluent.
- the gas-liquid separation is preferably performed in two stages, high temperature and low temperature. This can prevent clogging of the gas-liquid separation section 6 by heavy hydrocarbons.
- high-temperature gas-liquid separation can be performed at 80°C
- low-temperature gas-liquid separation can be performed at 40°C.
- the temperature during gas-liquid separation may be raised to a temperature 20° C. lower than the boiling point temperature of water at the partial pressure of water.
- Liquid components include oily components, including C5+ components, and aqueous components, including water and oxygenated hydrocarbons.
- Gaseous components include hydrogen, carbon monoxide, carbon dioxide and C4-components.
- the gas component separated by the gas-liquid separation section 6 is sent to the first separation section 10 .
- the first separation unit 10 separates hydrogen, carbon dioxide, and C4-components from gas components (first separation step). Carbon monoxide is included on the C4-component side. Note that carbon monoxide may be contained on the side of hydrogen and carbon dioxide.
- the first separation section 10 as an example performs separation using at least one of a pressure swing adsorption (PSA) method and a membrane separation method. When the first separation section 10 uses the membrane separation method, the first separation section 10 as an example has at least one of a polyimide film, a carbon film obtained by carbonizing the polyimide film, and a metal film containing Pd.
- PSA pressure swing adsorption
- the hydrogen and carbon dioxide separated in the first separation section 10 are sent to the reverse shift reaction section 2 .
- the reverse shift reaction section 2 receives the supply of hydrogen and carbon dioxide separated by the first separation section 10 and uses the hydrogen and carbon dioxide to generate synthesis gas.
- the utilization rate of hydrogen and carbon dioxide supplied as raw materials can be increased, and the production efficiency of C5+ components can be improved.
- the recycle gas supplied to the reverse shift reaction section 2 contains a large amount of compounds other than hydrogen and carbon dioxide, which are reactants in the reverse shift reaction section 2, an equilibrium composition is aimed in the reverse shift reaction section 2.
- a reverse reaction can occur.
- carbon monoxide production may be reduced.
- the reverse reaction can be suppressed by sending the hydrogen and carbon dioxide separated by the first separation unit 10 to the reverse shift reaction unit 2 . Therefore, the production efficiency of the C5+ component can be further improved.
- the C4- component and carbon monoxide separated in the first separation section 10 are sent to the contact reaction section 8.
- the catalytic reaction section 8 receives the C4-component separated by the first separation section 10 and uses the C4-component to generate hydrogen and carbon monoxide.
- the C4- component is sent to the reverse shift reaction unit 2 without providing the first separation unit 10 without providing the first separation unit 10.
- the C4- component is difficult to react in the reverse shift reaction unit 2 and accumulates in the system.
- the partial pressure of the syngas in the system decreases, and the reaction in the hydrocarbon production section 4 can be inhibited.
- the C4- component separated in the first separation section 10 is sent to the contact reaction section 8 and used to generate hydrogen and carbon monoxide.
- Carbon monoxide is also used for the reaction in the contact reaction section 8 .
- carbon dioxide does not participate in the reaction in the contact reaction section 8. Additionally, carbon dioxide is generally a non-flammable substance. Therefore, even when the contact reaction section 8 performs a partial oxidation reaction or an autothermal reforming reaction, which will be described later, carbon dioxide is not used for combustion. Therefore, when carbon dioxide is sent to the contact reaction section 8 without providing the first separation section 10, the carbon dioxide is also heated when the temperature of the contact reaction section 8 is raised to the reaction temperature of the contact reaction. , the required energy may increase. In contrast, in the present embodiment, the carbon dioxide separated in the first separation section 10 is sent to the reverse shift reaction section 2 and used to generate synthesis gas. As a result, an increase in the required energy in the contact reaction section 8 can be suppressed, and the production efficiency of the C5+ component can be further improved.
- the contact reaction section 8 produces hydrogen and carbon monoxide from C4-components by any of steam reforming reaction, partial oxidation reaction and autothermal reforming reaction.
- the catalytic reaction section 8 produces hydrogen and carbon monoxide from C4-components by a reforming reaction (at least one of a steam reforming reaction and an autothermal reforming reaction). If oxygen is required for the reaction that takes place in the contact reaction section 8, this oxygen is supplied from the water electrolysis module 20, for example.
- the catalytic reaction section 8 When the catalytic reaction section 8 produces hydrogen and carbon monoxide from C4-components in a steam reforming reaction, the catalytic reaction section 8 can be configured with a known steam reformer.
- the contact reaction section 8 as an example generates methane from the C4-component by a pre-stage reaction that performs a steam reforming reaction at a first temperature, and a steam reforming reaction at a second temperature higher than the first temperature.
- Carbon monoxide and hydrogen are produced from methane by the post-stage reaction of
- the contact reaction section 8 may include a reactor for the front-stage reaction and a reactor for the rear-stage reaction, or the temperature may be changed from the first temperature to the second temperature within one reactor.
- the first temperature is, for example, 450-600°C, preferably 450-500°C.
- the second temperature is, for example, 750° C. or higher.
- the difference in reaction temperature between the former stage and the latter stage is preferably 150° C. or higher, more preferably 250° C. or higher.
- C4-components with 2 or more carbon atoms When C4-components with 2 or more carbon atoms are directly subjected to a reforming reaction at a second temperature, each adjacent carbon atom is converted to carbon monoxide, and disproportionation occurs between adjacent carbon monoxides. A reaction occurs and coke (carbon) deposition is likely to occur.
- C4-components having 2 or more carbon atoms are highly likely to produce olefins by dehydrogenation reaction at 850° C. or less and deposit coke (heavy hydrocarbons) due to the polymerization thereof. Coke deposition may cause deterioration of the catalyst and clogging of the reactor.
- O/C ratio oxygen/carbon ratio
- the O/C ratio is the ratio of the number of moles (O) of oxygen atoms supplied into the contact reaction section 8 to the number of moles (C) of carbon atoms supplied into the contact reaction section 8 .
- the first temperature is set so that the preliminary reforming reaction represented by the following formulas (5) to (7) occurs as the first stage reaction and mainly produces methane.
- the S/C ratio is preferably 2.5 to 3.0.
- the reaction shown in equation (7) is an exothermic reaction. Therefore, if the composition and pressure are the same, the lower the temperature, the higher the yield of methane.
- the second temperature is set so that a reaction represented by the following formula (8) occurs as a post-stage reaction to produce synthesis gas containing carbon monoxide and hydrogen.
- the reaction shown in formula (8) is the reverse reaction of formula (7) and is an endothermic reaction. Therefore, if the composition and pressure are the same, the higher the temperature, the higher the yield of carbon monoxide and hydrogen.
- the S/C ratio at the second temperature is 1.0-2.5. It is preferable that the S/C ratio can be adjusted by not adding water that has been consumed in the previous reaction.
- the C4-component is denoted as C n H m , where n is an integer from 1-4 and m is an integer from 4-10. In the following reaction formulas, C4-components are similarly indicated.
- the catalytic reaction section 8 when the catalytic reaction section 8 produces hydrogen and carbon monoxide from C4-components by an autothermal reforming reaction, the catalytic reaction section 8 can be composed of a known autothermal reformer.
- the reaction represented by the following formula (9) first occurs, followed by the reaction represented by the following formula (10).
- the reaction shown in equation (9) is an exothermic reaction.
- the reaction represented by formula (10) is an endothermic reaction.
- the heat required for the reaction shown in formula (10) is covered by the heat generated in the reaction shown in formula (9).
- By-product oxygen generated in the water electrolysis module 20 can be used in the reaction represented by the formula (9).
- the catalytic reaction section 8 when the catalytic reaction section 8 produces hydrogen and carbon monoxide from the C4-component by partial oxidation reaction, the catalytic reaction section 8 can be constructed of a known partial oxidation reactor. In this case, the reaction represented by the following formula (11) occurs in the contact reaction section 8 . By-product oxygen generated in the water electrolysis module 20 can be used in the reaction represented by the formula (11). CnHm+( n /2) O2 ⁇ nCO+( m / 2 )H2 (11)
- a preliminary reformer (not shown) for performing the above-described preliminary reforming reaction is provided between the first separation section 10 and the contact reaction section 8. may be provided.
- This pre-reforming reaction is performed at the first temperature described above.
- the reactions shown in the above formulas (5) to (7) occur, the C4- component sent from the first separation unit 10 is reformed into methane by the pre-reformer, and this methane is self-heated. It can be subjected to reforming reaction.
- hydrogen and carbon monoxide can be produced while suppressing deterioration of the catalyst due to coke deposition as described above and suppressing an increase in the S/C ratio. Therefore, it is possible to further improve the production efficiency of the C5+ component.
- the effluent from the contact reaction section 8 is sent to the fifth separation section 18.
- This effluent may contain unreacted water as well as hydrogen and carbon monoxide.
- the fifth separation section 18 can consist of a known gas-liquid separator and separates hydrogen and carbon monoxide and water from the effluent.
- the water separated in the fifth separation section 18 is sent to the contact reaction section 8 and reused for the reaction in the contact reaction section 8 .
- the contact reaction section 8 performs only the partial oxidation reaction
- the supply of water from the fifth separation section 18 to the contact reaction section 8 is omitted.
- the contact reaction section 8 performs only the partial oxidation reaction
- the supply of water from the fourth separation section 16 described above and the supply of the aqueous component from the third separation section 14 described later are omitted.
- the hydrogen and carbon monoxide separated by the fifth separation unit 18 are sent to the hydrocarbon production unit 4.
- Hydrocarbon production unit 4 receives the supply of hydrogen and carbon monoxide produced by contact reaction unit 8, and uses the hydrogen and carbon monoxide to produce C5+ components. Thereby, the utilization rate of hydrogen and carbon dioxide supplied as raw materials can be improved, and the production efficiency of C5+ components can be improved.
- the liquid component separated by the gas-liquid separation section 6 is sent to the second separation section 12 .
- the 2nd separation part 12 can be comprised with a well-known oil-water separator, and separates an oil component and an aqueous component from a liquid component (2nd separation process).
- the C5+ component contained in the oily component separated in the second separation unit 12 is optionally upgraded by catalytic reforming, hydrocracking, hydrorefining, alkylation, isomerization, etc., for example, jet fuel, Used as a substitute for gasoline, kerosene, etc.
- the C4- The components may be returned to the first separation section 10 . As a result, it is possible to increase the production efficiency as a substitute for jet fuel or the like.
- a part of the aqueous component separated in the second separation section 12 is sent to the contact reaction section 8.
- the contact reaction section 8 receives the supply of the aqueous component separated by the second separation section 12 and also uses the aqueous component to generate hydrogen and carbon monoxide.
- water in the aqueous component can be converted to hydrogen in the contact reaction section 8 . Therefore, since the amount of hydrogen supplied as a raw material can be reduced, the production efficiency of C5+ components can be improved.
- oxygen-containing hydrocarbons in the aqueous component can be converted to carbon monoxide in the contact reaction section 8 . This also can improve the production efficiency of the C5+ component.
- part of the aqueous component separated by the second separation unit 12 is sent to the water electrolysis module 20 .
- the water electrolysis module 20 receives the aqueous component separated by the second separation unit 12 and uses the aqueous component to generate hydrogen.
- the aqueous component separated by the second separation section 12 is sent to the contact reaction section 8 and the water electrolysis module 20 via the third separation section 14 .
- the third separation section 14 separates at least part of the water from the aqueous component.
- water substantially free of oxygenated hydrocarbons and water in which oxygenated hydrocarbons are concentrated are obtained.
- water is purified.
- the third separation section 14 performs separation using at least one method of pressure swing adsorption (PSA), precision distillation, and membrane separation.
- PSA pressure swing adsorption
- the third separation section 14 uses a membrane separation method
- the third separation section 14 as an example has at least one of a reverse osmosis membrane, a zeolite membrane and a carbon membrane.
- the water separated by the third separation unit 14 that is, the water from which oxygen-containing hydrocarbons have been removed, in other words, purified water is supplied to the water electrolysis module 20 .
- the water electrolysis module 20 is supplied with the water separated by the third separation unit 14 and uses the water to generate hydrogen.
- catalyst deterioration in the water electrolysis module 20 can be suppressed. Therefore, the usage period of the water electrolysis module 20 can be extended, and the production efficiency of the C5+ component can be improved.
- the aqueous component from which the water is separated in the third separation section 14, in other words, the water in which the oxygenated hydrocarbons are concentrated is supplied to the contact reaction section 8.
- the contact reaction section 8 receives the aqueous component from which the water is separated by the third separation section 14, and uses the aqueous component to generate hydrogen and carbon monoxide.
- the catalytic reaction section 8 produces hydrogen and carbon monoxide from the oxygen-containing hydrocarbons by reforming reaction.
- the catalytic reaction section 8 When the catalytic reaction section 8 produces hydrogen and carbon monoxide from oxygen-containing hydrocarbons in a steam reforming reaction, the catalytic reaction section 8 can be configured with a known steam reformer.
- the contact reaction section 8 as an example generates methane from the oxygenated hydrocarbon by a pre-stage reaction that performs a steam reforming reaction at a first temperature, and steam reforming at a second temperature higher than the first temperature.
- Carbon monoxide and hydrogen are produced from methane by a post-stage reaction that reacts.
- the first temperature is, for example, 450-600°C, preferably 450-500°C.
- the second temperature is, for example, 750° C. or higher.
- the difference in reaction temperature between the former stage and the latter stage is preferably 150° C. or higher, more preferably 250° C. or higher.
- the reaction temperature in the former stage can be lower than the reaction temperature in the latter stage.
- the reaction temperature in the preceding stage can be further lowered than in the case of the C4-component.
- the first temperature is set so that the preliminary reforming reaction represented by the following formulas (12) to (14) occurs as the first-stage reaction to mainly produce methane.
- the S/C ratio is preferably 2.5 to 3.0.
- the reaction shown in equation (14) is an exothermic reaction. Therefore, if the composition and pressure are the same, the lower the temperature, the higher the yield of methane.
- the second temperature is set so that a reaction represented by the following formula (15) occurs as a post-stage reaction to produce synthesis gas containing carbon monoxide and hydrogen.
- the reaction shown in formula (15) is the reverse reaction of formula (14) and is also an endothermic reaction. Therefore, if the composition and pressure are the same, the higher the temperature, the higher the yield of carbon monoxide and hydrogen.
- the S/C ratio at the second temperature is 1.0-2.5. It is preferable that the S/C ratio can be adjusted by not adding water that has been consumed in the previous reaction.
- n is an integer from 1 to 7
- m is an integer from 4 to 16, for example.
- the values of n and m in oxygenated hydrocarbons are the same.
- the catalytic reaction section 8 when the catalytic reaction section 8 produces hydrogen and carbon monoxide from oxygen-containing hydrocarbons by an autothermal reforming reaction, the catalytic reaction section 8 can be configured with a known autothermal reformer.
- the reaction represented by the following formula (16) first occurs, followed by the reaction represented by the following formula (17).
- the reaction shown in equation (16) is an exothermic reaction.
- the reaction represented by formula (17) is an endothermic reaction.
- the heat required for the reaction shown in formula (17) is covered by the heat generated in the reaction shown in formula (16).
- By-product oxygen generated in the water electrolysis module 20 can be used in the reaction represented by the formula (16).
- a preliminary reformer (not shown) for performing the above preliminary reforming reaction is provided between the third separation section 14 and the contact reaction section 8. may be provided.
- This pre-reforming reaction is performed at the first temperature described above.
- the reactions shown in the above formulas (12) to (14) occur, the oxygen-containing hydrocarbons sent from the third separation unit 14 are reformed into methane by the steam reformer, and this methane is self-reformed. It can be subjected to thermal reforming reaction.
- hydrogen and carbon monoxide can be produced while suppressing deterioration of the catalyst due to coke deposition as described above and suppressing an increase in the S/C ratio. Therefore, it is possible to further improve the production efficiency of the C5+ component.
- the dehydration reaction represented by the following formula (18) and the dehydration condensation reaction represented by the formula (19) occur as side reactions, and water can be produced from the hydrogen-containing hydrocarbon.
- the numerical range of a is the same as that of n
- the numerical range of b is the same as that of m.
- the amount of water supplied to the contact reaction section 8 is reduced by separating at least part of the water in the third separation section 14 .
- the S/C ratio in the contact reaction section 8 can be reduced.
- this by-product water can be used to suppress coke deposition. Therefore, while reducing the amount of water supplied to the contact reaction section 8 to reduce the S/C ratio, coke deposition can be suppressed and the deterioration of the catalyst in the contact reaction section 8 can be suppressed. As a result, the period of use of the contact reaction section 8 can be extended, and the production efficiency of the C5+ component can be improved.
- the energy efficiency for the production of C5+ components can be expressed by the following equation (20).
- Energy efficiency calorific value of obtained C5+ component / (calorific value of raw material hydrogen consumed + necessary heat quantity required for heat recovery for production + consumed electric power required for production of raw material hydrogen + recovery of consumed raw material carbon dioxide required heat and power) (20)
- the "necessary amount of heat required for heat recovery for manufacturing" in the formula (20) is based on the assumption that the heat corresponding to the temperature difference between the inlet gas and the outlet gas in each reaction section is recovered and the recovered heat is reused for the reaction. means the amount of heat applied from outside the system.
- the raw material supplied to the reverse shift reaction section 2 needs to be heated to the reaction temperature (eg, 800° C.) in the reverse shift reaction section 2 .
- the reverse shift reaction is an endothermic reaction, it is necessary to add heat.
- the synthesis gas needs to be cooled. Therefore, the heat of the synthesis gas (outlet gas) discharged from the reverse shift reaction unit 2 is recovered by a heat exchanger, and the recovered heat is transferred to the raw material (inlet gas).
- the fuel for the heating furnace for heating the raw material and the electric power for the chiller for cooling the synthesis gas can be reduced.
- the carbon dioxide recovery unit 22 separates and recovers carbon dioxide by a chemical adsorption method or the like, heat is required to dissipate the adsorbed carbon dioxide.
- the FT reaction occurring in the hydrocarbon production section 4 is an exothermic reaction. Therefore, the heat generated in the hydrocarbon production section 4 can be recovered by the heat exchanger, and the recovered heat can be used for the diffusion of carbon dioxide in the carbon dioxide recovery section 22 .
- the contact reaction section 8 is composed of an autothermal reformer, the required amount of heat can be reduced compared to when it is composed of a steam reformer.
- the contact reaction section 8 is composed of an autothermal reformer
- hydrogen and carbon dioxide are supplied to the contact reaction section 8 without providing the first separation section 10
- heat is required to heat the carbon dioxide, It becomes difficult to cover the reaction heat required for the reforming reaction by partial oxidation of the C4-component.
- the insufficient heat of reaction is covered by the combustion of hydrogen sent to the catalytic reaction section 8 together with carbon dioxide.
- the catalytic reaction section 8 is composed of a steam reformer, combustion of hydrogen does not occur in the catalytic reaction section 8 and by-product water is not produced. Therefore, even if hydrogen is supplied to the contact reaction section 8 , the water recycled from the hydrocarbon production section 4 is used for the reforming reaction in the contact reaction section 8 . Therefore, the H 2 /CO 2 ratio of the fresh feed can be made smaller than when the catalytic reaction section 8 is configured with an autothermal reformer. If the H 2 /CO 2 ratio of the fresh feed can be reduced, the power required to produce hydrogen can be reduced. Therefore, it is possible to suppress the decrease in the energy efficiency shown in Equation (20).
- the contact reaction section 8 is composed of a steam reformer, the effect of improving the production efficiency of the C5+ component by recycling the aqueous component can be exhibited more strongly. Further, when the contact reaction section 8 is composed of an autothermal reformer, combining the first separation section 10 can make it easier to exhibit the improvement effect.
- the molar ratio ( CO/H2 ratio) between carbon monoxide and hydrogen supplied to the hydrocarbon production unit 4 is preferably 1.5 or more and 4.0 or less. , is more preferably 2.0 or more and 3.5 or less, and more preferably 2.2 or more and 3.0 or less.
- the S/C ratio in the first stage reaction is preferably 3.0 or more and 6.0 or less.
- the S/C ratio in the latter reaction is preferably 0.5 or more and 3.0 or less, more preferably 1.0 or more and 2.5 or less.
- FIG. 2 is a schematic diagram of a hydrocarbon production apparatus according to a comparative example.
- 3 is a schematic diagram of a hydrocarbon production apparatus according to Test Example 1.
- FIG. 4 is a schematic diagram of a hydrocarbon production apparatus according to Test Example 2.
- FIG. 5 is a schematic diagram of a hydrocarbon production apparatus according to Test Example 3.
- FIG. 6 is a schematic diagram of a hydrocarbon production apparatus according to Test Example 4.
- the hydrocarbon production apparatus does not include the contact reaction section 8 and the first separation section 10. Therefore, the gas component separated by the gas-liquid separation section 6 is recycled to the reverse shift reaction section 2 as it is. Also, the third separation section 14 is not provided. Therefore, separation of water from the aqueous component separated by the second separation section 12, that is, concentration treatment of oxygenated hydrocarbons is not performed.
- the hydrocarbon production apparatus does not include the first separation section 10 . Therefore, the gas components separated by the gas-liquid separation section 6 are recycled to the contact reaction section 8 as they are. Further, the contact reaction section 8 is composed of an autothermal reformer (ATR). Also, the hydrogen, carbon monoxide and carbon dioxide separated in the fifth separation section 18 are recycled to the reverse shift reaction section 2 . Further, a third separating section 14 is provided. Therefore, the aqueous component separated in the second separation section 12 is subjected to oxygenated hydrocarbon concentration treatment. Then, the water in which the oxygen-containing hydrocarbons are concentrated is recycled to the contact reaction section 8 .
- ATR autothermal reformer
- the hydrocarbon production apparatus has a first separation section 10 .
- the C4- component and carbon monoxide separated in the first separation section 10 are recycled to the contact reaction section 8 .
- the hydrogen and carbon dioxide separated in the first separation section 10 are recycled to the reverse shift reaction section 2 .
- the contact reaction section 8 is composed of an autothermal reformer.
- the hydrogen and carbon monoxide separated in the fifth separation section 18 are recycled to the hydrocarbon production section 4 .
- a third separation section 14 is also provided. Therefore, the aqueous component separated in the second separation section 12 is subjected to oxygenated hydrocarbon concentration treatment. Then, the water in which the oxygen-containing hydrocarbons are concentrated is recycled to the contact reaction section 8 .
- the hydrocarbon production apparatus does not include the first separation section 10 . Therefore, the gas components separated by the gas-liquid separation section 6 are recycled to the contact reaction section 8 as they are. Further, the contact reaction section 8 is composed of a steam reformer (SR). Also, the hydrogen, carbon monoxide and carbon dioxide separated in the fifth separation section 18 are recycled to the reverse shift reaction section 2 . Further, a third separating section 14 is provided. Therefore, the aqueous component separated in the second separation section 12 is subjected to oxygenated hydrocarbon concentration treatment. Then, the water in which the oxygen-containing hydrocarbons are concentrated is recycled to the contact reaction section 8 .
- SR steam reformer
- the hydrocarbon production apparatus has a first separation section 10 .
- the C4- component and carbon monoxide separated in the first separation section 10 are recycled to the contact reaction section 8 .
- the hydrogen and carbon dioxide separated in the first separation section 10 are recycled to the reverse shift reaction section 2 .
- the contact reaction section 8 is composed of a steam reformer.
- the hydrogen and carbon monoxide separated in the fifth separation section 18 are recycled to the hydrocarbon production section 4 .
- a third separation section 14 is also provided. Therefore, the aqueous component separated in the second separation section 12 is subjected to oxygenated hydrocarbon concentration treatment. Then, the water in which the oxygen-containing hydrocarbons are concentrated is recycled to the contact reaction section 8 .
- reaction conditions for calculating the energy efficiency were as follows. In addition to the reaction conditions below, the H 2 /CO 2 ratio of the fresh feed was adjusted so that the H 2 /CO 2 ratio (molar ratio) supplied to the reverse shift reaction section was maintained at 3. Each reaction was allowed to proceed until the equilibrium composition was reached, except for the FT reaction in the hydrocarbon production section.
- Reaction temperature of reverse shift reaction section 800°C Reaction temperature of hydrocarbon production department: 200°C Reaction temperature of autothermal reformer or steam reformer: 880°C Reaction pressure (constant in the system): 4 MPa
- the energy efficiency in the comparative example was set to 1 for the case where the aqueous component separated in the second separation unit 12 or the water separated in the third separation unit 14 was recycled to the water electrolysis module 20 and the case where it was not recycled.
- the energy efficiency in each test example was compared. The results were as follows.
- Test Example 1 When not recycling the aqueous component Comparative example: 1.00 Test Example 1: 1.05 Test Example 2: 1.17 Test Example 3: 0.99 Test Example 4: 1.19 When the aqueous component is recycled Comparative example: 1.00 Test Example 1: 1.03 Test Example 2: 1.13 Test Example 3: 1.12 Test Example 4: 1.34
- Embodiments may be specified by items described below.
- a reverse shift reaction section (2) for reducing carbon dioxide to carbon monoxide by a reverse shift reaction using carbon dioxide and hydrogen as raw material gases to obtain a synthesis gas containing carbon monoxide and hydrogen;
- a hydrocarbon production unit (4) that produces hydrocarbons (C5+) using synthesis gas;
- a contact reaction section (8) that receives the supply of the light hydrocarbons (C4-) separated by the first separation section (10) and produces hydrogen and carbon monoxide using the light hydrocarbons (C4-); with The reverse shift reaction section (2) receives the supply of
- a hydrocarbon production device (1) [Item 2]
- the liquid component includes an oil component containing hydrocarbons having 5 or more carbon atoms (C5+) and an aqueous component containing water
- the catalytic reaction section (8) produces hydrogen and carbon monoxide from light hydrocarbons (C4-) through a reforming reaction
- the hydrocarbon production device (1) comprises a second separation section (12) for separating the aqueous component from the liquid component
- the contact reaction section (8) receives the supply of the aqueous component separated by the second separation section (12), and also uses the aqueous component to generate hydrogen and carbon monoxide.
- a hydrocarbon production apparatus (1) according to item 1.
- the aqueous component also includes hydrophilic oxygenated hydrocarbons that are soluble in water
- the hydrocarbon production device (1) comprises a third separation section (14) for separating at least part of the water from the aqueous component
- the contact reaction section (8) receives the supply of the aqueous component from which the water is separated by the third separation section (14), and uses the aqueous component to generate hydrogen and carbon monoxide.
- a hydrocarbon production apparatus (1) according to item 2.
- the catalytic reaction section (8) produces methane from light hydrocarbons (C4-) through a reforming reaction at a first temperature, and produces carbon monoxide from methane through a reforming reaction at a second temperature higher than the first temperature. and producing hydrogen, 4.
- a hydrocarbon production apparatus (1) according to any one of items 1 to 3.
- a reverse shift reaction step of using carbon dioxide and hydrogen as raw material gases and reducing the carbon dioxide to carbon monoxide by a reverse shift reaction to obtain a synthesis gas containing carbon monoxide and hydrogen;
- a gaseous component containing hydrogen, carbon dioxide and light hydrocarbons having 4 or less carbon atoms (C4-) and a liquid component containing hydrocarbons having 5 or more carbon atoms (C5+) are removed from an effluent from a hydrocarbon production process.
- the reverse shift reaction step the hydrogen and carbon dioxide separated in the first separation step are supplied, and the hydrogen and carbon dioxide are also used to generate synthesis gas
- the hydrocarbon production step the hydrogen and carbon monoxide produced in the catalytic reaction step are supplied, and the hydrogen and carbon monoxide are also used to produce hydrocarbons (C5+). Hydrocarbon production method.
- the liquid component includes an oil component containing hydrocarbons having 5 or more carbon atoms (C5+) and an aqueous component containing water
- the hydrocarbon production method includes a second separation step of separating the aqueous component from the liquid component, In the contact reaction step, the aqueous component separated in the second separation step is supplied, and the aqueous component is also used to generate hydrogen and carbon monoxide. 6.
- the present invention can be used for hydrocarbon production equipment and hydrocarbon production methods.
- 1 hydrocarbon production device 2 reverse shift reaction section, 4 hydrocarbon production section, 6 gas-liquid separation section, 8 contact reaction section, 10 first separation section, 12 second separation section, 14 third separation section, 16 fourth Separation section, 18 Fifth separation section, 20 Water electrolysis module, 22 Carbon dioxide recovery section.
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Abstract
Description
酸素発生電極で起こる反応:2H2O→O2+4H++4e- (1)
水素発生電極で起こる反応:4H++4e-→2H2 (2)
H2+CO2→CO+H2O (3)
nCO+(2n+1)H2→CnH2n+2+nH2O (4)
気液分離部6で分離された気体成分は、第1分離部10に送られる。第1分離部10は、気体成分から、水素および二酸化炭素と、C4-成分とを分離する(第1分離工程)。一酸化炭素は、C4-成分側に含まれる。なお、一酸化炭素は、水素および二酸化炭素側に含まれる場合もある。一例としての第1分離部10は、圧力変動吸着(PSA)法および膜分離法の少なくとも一方を用いて分離を行う。第1分離部10が膜分離法を用いる場合、一例としての第1分離部10は、ポリイミド膜、ポリイミド膜を炭化させた炭素膜、およびPdを含む金属膜の少なくとも1つを有する。
CnHm+nH2O→nCO+(n+m/2)H2 (5)
CO+H2O→CO2+H2 (6)
CO+3H2→CH4+H2O (7)
CH4+H2O→CO+3H2 (8)
CnHm+(n/2)O2→nCO+(m/2)H2 (9)
CnHm+nH2O→nCO+(n+m/2)H2 (10)
CnHm+(n/2)O2→nCO+(m/2)H2 (11)
気液分離部6で分離された液体成分は、第2分離部12に送られる。第2分離部12は、公知の油水分離器で構成することができ、液体成分から油性成分と、水性成分とを分離する(第2分離工程)。第2分離部12で分離された油性成分に含まれるC5+成分は、必要に応じて接触改質、水素化分解、水素化精製、アルキル化、異性化等によるアップグレード処理を経て、例えばジェット燃料、ガソリン、灯油等の代替品として利用される。硫黄や窒素などのヘテロ元素を含む原油由来の油性成分の処理がアップグレード装置でなされず、よって原油由来のガス成分がアップグレード装置からの流出物に含まれない場合、アップグレード装置で副生したC4-成分を第1分離部10に戻してもよい。これにより、ジェット燃料等の代替品としての製造効率を高めることができる。
CnHmO+(n-1)H2O=nCO+(n-1+m/2)H2 (12)
CO+H2O→CO2+H2 (13)
CO+3H2→CH4+H2O (14)
CH4+H2O→CO+3H2 (15)
CnHmO+{(n-1)/2}O2→nCO+(m/2)H2 (16)
CnHmO+(n-1)H2O=nCO+(n-1+m/2)H2 (17)
CnHmO=CnHm-2+H2O (18)
CnHmO+CaHbO=CnHm-1OCaHb-1+H2O (19)
エネルギー効率=得られたC5+成分の発熱量/(消費した原料水素の発熱量+製造にかかる熱回収前提の必要熱量+消費した原料水素の製造に必要な電力+消費した原料二酸化炭素の回収に必要な熱量および電力) (20)
式(20)中の「製造にかかる熱回収前提の必要熱量」とは、各反応部における入口ガスと出口ガスの温度差分の熱を回収し、回収した熱を反応に再利用することを前提として、系外から加える熱量を意味する。
逆シフト反応部の反応温度:800℃
炭化水素製造部の反応温度:200℃
自己熱改質器または水蒸気改質器の反応温度:880℃
反応圧力(系内において一定):4MPa
比較例:1.00
試験例1:1.05
試験例2:1.17
試験例3:0.99
試験例4:1.19
水性成分のリサイクルを行った場合
比較例:1.00
試験例1:1.03
試験例2:1.13
試験例3:1.12
試験例4:1.34
[項目1]
原料ガスとしての二酸化炭素および水素を用いて、逆シフト反応によって二酸化炭素を一酸化炭素に還元し、一酸化炭素および水素を含む合成ガスを得る逆シフト反応部(2)と、
合成ガスを用いて炭化水素(C5+)を製造する炭化水素製造部(4)と、
炭化水素製造部(4)からの流出物から、水素、二酸化炭素および炭素数4以下の軽質炭化水素(C4-)を含む気体成分と、炭素数5以上の炭化水素(C5+)を含む液体成分と、を分離する気液分離部(6)と、
気体成分から、水素および二酸化炭素と、軽質炭化水素(C4-)と、を分離する第1分離部(10)と、
第1分離部(10)が分離した軽質炭化水素(C4-)の供給を受けて、当該軽質炭化水素(C4-)を用いて水素および一酸化炭素を生成する接触反応部(8)と、を備え、
逆シフト反応部(2)は、第1分離部(10)が分離した水素および二酸化炭素の供給を受けて、当該水素および二酸化炭素も合成ガスの生成に用い、
炭化水素製造部(4)は、接触反応部(8)が生成した水素および一酸化炭素の供給を受けて、当該水素および一酸化炭素も炭化水素(C5+)の製造に用いる、
炭化水素製造装置(1)。
[項目2]
液体成分は、炭素数5以上の炭化水素(C5+)を含む油性成分と、水を含む水性成分とを含み、
接触反応部(8)は、改質反応により軽質炭化水素(C4-)から水素および一酸化炭素を生成し、
炭化水素製造装置(1)は、液体成分から水性成分を分離する第2分離部(12)を備え、
接触反応部(8)は、第2分離部(12)が分離した水性成分の供給を受けて、当該水性成分も水素および一酸化炭素の生成に用いる、
項目1に記載の炭化水素製造装置(1)。
[項目3]
水性成分は、水に溶解する親水性の含酸素炭化水素も含み、
炭化水素製造装置(1)は、水性成分から少なくとも一部の水を分離する第3分離部(14)を備え、
接触反応部(8)は、第3分離部(14)により水が分離された水性成分の供給を受けて、当該水性成分を水素および一酸化炭素の生成に用いる、
項目2に記載の炭化水素製造装置(1)。
[項目4]
接触反応部(8)は、第1温度での改質反応により軽質炭化水素(C4-)からメタンを生成し、第1温度よりも高い第2温度での改質反応によりメタンから一酸化炭素および水素を生成する、
項目1乃至3のいずれかに記載の炭化水素製造装置(1)。
[項目5]
原料ガスとしての二酸化炭素および水素を用いて、逆シフト反応によって二酸化炭素を一酸化炭素に還元し、一酸化炭素および水素を含む合成ガスを得る逆シフト反応工程と、
合成ガスを用いて炭化水素(C5+)を製造する炭化水素製造工程と、
炭化水素製造工程からの流出物から、水素、二酸化炭素および炭素数4以下の軽質炭化水素(C4-)を含む気体成分と、炭素数5以上の炭化水素(C5+)を含む液体成分と、を分離する気液分離工程と、
気体成分から、水素および二酸化炭素と、軽質炭化水素(C4-)と、を分離する第1分離工程と、
第1分離工程で分離した軽質炭化水素(C4-)の供給を受けて、当該軽質炭化水素(C4-)を用いて水素および一酸化炭素を生成する接触反応工程と、を含み、
逆シフト反応工程では、第1分離工程で分離した水素および二酸化炭素の供給を受けて、当該水素および二酸化炭素も合成ガスの生成に用い、
炭化水素製造工程では、接触反応工程で生成した水素および一酸化炭素の供給を受けて、当該水素および一酸化炭素も炭化水素(C5+)の製造に用いる、
炭化水素製造方法。
[項目6]
液体成分は、炭素数5以上の炭化水素(C5+)を含む油性成分と、水を含む水性成分とを含み、
接触反応工程では、改質反応により軽質炭化水素(C4-)から水素および一酸化炭素を生成し、
炭化水素製造方法は、液体成分から水性成分を分離する第2分離工程を含み、
接触反応工程では、第2分離工程で分離した水性成分の供給を受けて、当該水性成分も水素および一酸化炭素の生成に用いる、
項目5に記載の炭化水素製造方法。
Claims (6)
- 原料ガスとしての二酸化炭素および水素を用いて、逆シフト反応によって二酸化炭素を一酸化炭素に還元し、一酸化炭素および水素を含む合成ガスを得る逆シフト反応部と、
前記合成ガスを用いて炭化水素を製造する炭化水素製造部と、
前記炭化水素製造部からの流出物から、水素、二酸化炭素および炭素数4以下の軽質炭化水素を含む気体成分と、炭素数5以上の炭化水素を含む液体成分と、を分離する気液分離部と、
前記気体成分から、水素および二酸化炭素と、軽質炭化水素と、を分離する第1分離部と、
前記第1分離部が分離した軽質炭化水素の供給を受けて、当該軽質炭化水素を用いて水素および一酸化炭素を生成する接触反応部と、を備え、
前記逆シフト反応部は、前記第1分離部が分離した水素および二酸化炭素の供給を受けて、当該水素および二酸化炭素も前記合成ガスの生成に用い、
前記炭化水素製造部は、前記接触反応部が生成した水素および一酸化炭素の供給を受けて、当該水素および一酸化炭素も前記炭化水素の製造に用いる、
炭化水素製造装置。 - 前記液体成分は、炭素数5以上の炭化水素を含む油性成分と、水を含む水性成分とを含み、
前記接触反応部は、改質反応により前記軽質炭化水素から水素および一酸化炭素を生成し、
前記炭化水素製造装置は、前記液体成分から水性成分を分離する第2分離部を備え、
前記接触反応部は、前記第2分離部が分離した水性成分の供給を受けて、当該水性成分も水素および一酸化炭素の生成に用いる、
請求項1に記載の炭化水素製造装置。 - 前記水性成分は、水に溶解する親水性の含酸素炭化水素も含み、
前記炭化水素製造装置は、前記水性成分から少なくとも一部の水を分離する第3分離部を備え、
前記接触反応部は、前記第3分離部により水が分離された水性成分の供給を受けて、当該水性成分を水素および一酸化炭素の生成に用いる、
請求項2に記載の炭化水素製造装置。 - 前記接触反応部は、第1温度での改質反応により前記軽質炭化水素からメタンを生成し、前記第1温度よりも高い第2温度での改質反応により前記メタンから一酸化炭素および水素を生成する、
請求項1乃至3のいずれか1項に記載の炭化水素製造装置。 - 原料ガスとしての二酸化炭素および水素を用いて、逆シフト反応によって二酸化炭素を一酸化炭素に還元し、一酸化炭素および水素を含む合成ガスを得る逆シフト反応工程と、
前記合成ガスを用いて炭化水素を製造する炭化水素製造工程と、
前記炭化水素製造工程からの流出物から、水素、二酸化炭素および炭素数4以下の軽質炭化水素を含む気体成分と、炭素数5以上の炭化水素を含む液体成分と、を分離する気液分離工程と、
前記気体成分から、水素および二酸化炭素と、軽質炭化水素と、を分離する第1分離工程と、
前記第1分離工程で分離した軽質炭化水素の供給を受けて、当該軽質炭化水素を用いて水素および一酸化炭素を生成する接触反応工程と、を含み、
前記逆シフト反応工程では、前記第1分離工程で分離した水素および二酸化炭素の供給を受けて、当該水素および二酸化炭素も前記合成ガスの生成に用い、
前記炭化水素製造工程では、前記接触反応工程で生成した水素および一酸化炭素の供給を受けて、当該水素および一酸化炭素も前記炭化水素の製造に用いる、
炭化水素製造方法。 - 前記液体成分は、炭素数5以上の炭化水素を含む油性成分と、水を含む水性成分とを含み、
前記接触反応工程では、改質反応により前記軽質炭化水素から水素および一酸化炭素を生成し、
前記炭化水素製造方法は、前記液体成分から水性成分を分離する第2分離工程を含み、
前記接触反応工程では、前記第2分離工程で分離した水性成分の供給を受けて、当該水性成分も水素および一酸化炭素の生成に用いる、
請求項5に記載の炭化水素製造方法。
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JP2008248179A (ja) | 2007-03-30 | 2008-10-16 | Kitakyushu Foundation For The Advancement Of Industry Science & Technology | 一酸化炭素の還元による炭化水素の製造方法 |
US20100177861A1 (en) * | 2009-01-13 | 2010-07-15 | Areva Sa | System and a process for producing at least one hydrocarbon fuel from a carbonaceous material |
JP2014517806A (ja) * | 2011-02-22 | 2014-07-24 | アレバ | 改質段階を含み、動作条件が選択的に調整される、炭素材料からメタノール又は炭化水素を製造する方法 |
US20180093888A1 (en) * | 2015-04-29 | 2018-04-05 | Aghaddin Mamedov | Methods for conversion of co2 into syngas |
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2021
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- 2022-06-03 AU AU2022294462A patent/AU2022294462A1/en active Pending
- 2022-06-03 WO PCT/JP2022/022612 patent/WO2022264836A1/ja active Application Filing
- 2022-06-03 EP EP22824828.2A patent/EP4357327A1/en active Pending
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JP2008248179A (ja) | 2007-03-30 | 2008-10-16 | Kitakyushu Foundation For The Advancement Of Industry Science & Technology | 一酸化炭素の還元による炭化水素の製造方法 |
US20100177861A1 (en) * | 2009-01-13 | 2010-07-15 | Areva Sa | System and a process for producing at least one hydrocarbon fuel from a carbonaceous material |
JP2014517806A (ja) * | 2011-02-22 | 2014-07-24 | アレバ | 改質段階を含み、動作条件が選択的に調整される、炭素材料からメタノール又は炭化水素を製造する方法 |
US20180093888A1 (en) * | 2015-04-29 | 2018-04-05 | Aghaddin Mamedov | Methods for conversion of co2 into syngas |
Cited By (2)
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JP7361142B2 (ja) | 2022-01-12 | 2023-10-13 | 本田技研工業株式会社 | 燃料合成装置 |
US11931712B2 (en) | 2022-01-12 | 2024-03-19 | Honda Motor Co., Ltd. | Fuel synthesis device |
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JP2022191870A (ja) | 2022-12-28 |
EP4357327A1 (en) | 2024-04-24 |
AU2022294462A1 (en) | 2024-01-25 |
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