WO2021186658A1 - Système de production de méthanol et procédé de production de méthanol - Google Patents

Système de production de méthanol et procédé de production de méthanol Download PDF

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WO2021186658A1
WO2021186658A1 PCT/JP2020/012205 JP2020012205W WO2021186658A1 WO 2021186658 A1 WO2021186658 A1 WO 2021186658A1 JP 2020012205 W JP2020012205 W JP 2020012205W WO 2021186658 A1 WO2021186658 A1 WO 2021186658A1
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methanol
carbon monoxide
gas
methanol production
carbon dioxide
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PCT/JP2020/012205
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English (en)
Japanese (ja)
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晃平 吉川
篤 宇根本
杉政　昌俊
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株式会社日立製作所
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to a methanol production system and a methanol production method.
  • Patent Document 1 The technique described in Patent Document 1 is known as a method for producing carbon monoxide from carbon dioxide and producing methanol using the produced carbon monoxide.
  • the method for producing hydrogen described in Patent Document 1 is selected from (a) a metal selected from one of a group of metals belonging to Group IIIb of the Periodic Table and a group of metals belonging to Group IVa, or a group of both.
  • Patent Document 1 Since the reaction for synthesizing methanol from carbon monoxide is an exothermic reaction, the methanol discharged from the methanol production equipment has heat. Therefore, the technique described in Patent Document 1, which does not disclose the treatment of the discharged methanol, has room for improvement in terms of thermal efficiency.
  • the problem to be solved by the present invention is to provide a methanol production system and a methanol production method capable of improving thermal efficiency.
  • the methanol production system of the present invention comprises a carbon monoxide production apparatus for producing carbon monoxide from a first raw material gas containing carbon dioxide, and a carbon monoxide-containing gas containing carbon monoxide produced by the carbon monoxide production apparatus. It is provided with a methanol production apparatus for producing methanol using the above, and a first heat exchanger for transferring the heat of the produced gas containing methanol produced by the methanol production apparatus to the first raw material gas.
  • a carbon monoxide production apparatus for producing carbon monoxide from a first raw material gas containing carbon dioxide
  • a carbon monoxide-containing gas containing carbon monoxide produced by the carbon monoxide production apparatus It is provided with a methanol production apparatus for producing methanol using the above, and a first heat exchanger for transferring the heat of the produced gas containing methanol produced by the methanol production apparatus to the first raw material gas.
  • the present invention is not limited to the following contents and the illustrated contents, and can be arbitrarily modified and carried out within a range that does not significantly impair the effects of the present invention.
  • the present invention can be implemented by combining different embodiments. In the following description, the same members will be designated by the same reference numerals in different embodiments, and redundant description will be omitted.
  • FIG. 1 is a system diagram showing the methanol production system 100 of the first embodiment.
  • the methanol production system 100 produces carbon monoxide using carbon dioxide, and produces methanol using the produced carbon monoxide.
  • the methanol production system 100 includes a compression device 1, a first heat exchanger 2, a carbon monoxide production device 3, a compression device 4, a methanol production device 5, and a methanol recovery device 6.
  • the compression device 1 compresses the first raw material gas containing carbon dioxide.
  • the pressure of the first raw material gas can be set to a pressure suitable for carbon monoxide production in the carbon monoxide production apparatus 3 described later (for example, 800 hPa or more and 1200 hPa or less).
  • the first raw material gas is, for example, mixed with carbon dioxide and hydrogen stored in a carbon dioxide tank and a hydrogen tank (neither shown), and then supplied to the compression device 1 through the first raw material gas system 21.
  • the first source gas further contains hydrogen.
  • Hydrogen can be produced, for example, by electrolyzing water using renewable energy.
  • hydrogen for example, hydrogen generated by reforming can be used to carry out a Fischer-Tropsch reaction, and surplus hydrogen at that time can also be used.
  • the first heat exchanger 2 transfers the heat of the generated gas containing methanol produced by the methanol production apparatus 5 (described later) to the first raw material gas.
  • the first heat exchanger 2 is connected to the compression device 1 by the first raw material gas system 21. Details will be described later, but since methanol is produced by an exothermic reaction in the methanol production apparatus 5, the produced gas containing the produced methanol has heat. Therefore, in the first heat exchanger 2, the heat of the generated gas is used for heating the first raw material gas.
  • the heating is preferably performed so that the temperature of the first raw material gas is, for example, 200 ° C. or higher and 250 ° C. or lower. If necessary, an auxiliary heating facility may be provided.
  • the carbon monoxide production apparatus 3 produces carbon monoxide from the first raw material gas.
  • the carbon monoxide production apparatus 3 is connected to the first heat exchanger 2 by the first raw material gas system 21.
  • the carbon monoxide-containing gas containing the produced carbon monoxide can be obtained by the carbon monoxide production apparatus 3.
  • the carbon monoxide production apparatus 3 will be described with reference to FIG.
  • FIG. 2 is a schematic view showing the carbon monoxide production apparatus 3.
  • the carbon monoxide production apparatus 3 includes a reaction apparatus 31 and a decompression apparatus 32.
  • the reaction device 31 includes a granular reverse shift catalyst 34 and a granular adsorbent 35 inside a cylindrical housing 33 having openings 33a and 33b.
  • the adsorbent 35 is an example of the water removing mechanism 36, which will be described in detail later.
  • the reverse shift catalyst 34 and the adsorbent 35 are shown with a gap for simplification of the illustration.
  • the reverse shift catalyst 34 exhibits catalytic activity at, for example, 550 ° C. or lower (preferably 500 ° C. or lower), and promotes the reverse shift reaction represented by the following reaction formula (1).
  • the reaction represented by the formula (1) is an endothermic reaction. CO 2 + H 2 ⁇ CO + H 2 O... Reaction equation (1) That is, the carbon monoxide production apparatus 3 includes a reverse shift catalyst 34 that exhibits catalytic activity at 550 ° C. or lower. By including the reverse shift catalyst, carbon monoxide can be produced from carbon dioxide at a relatively low temperature such as 550 ° C. or lower.
  • the reverse shift catalyst 34 preferably contains at least one element of Cu, Co, or Mn as an active ingredient. By having these elements, carbon monoxide can be selectively produced, and the reverse shift reaction can proceed efficiently.
  • the precursor of the active ingredient include nitrates, acetates, chlorides, hydroxides and the like of each element.
  • an impregnation method, a coprecipitation method, a kneading method, a mechanical alloying method, a vapor deposition method and the like can be considered.
  • the form of the active ingredient is preferably an oxide or a metal alone.
  • Examples of the method for obtaining the oxide of the active ingredient include firing in a gas atmosphere containing oxygen such as in the atmosphere.
  • Examples of the method for obtaining the active component of a simple substance include a method in which firing is performed in the atmosphere to form an oxide, and then a reduction treatment is performed in a gas atmosphere containing hydrogen.
  • the active ingredient may be filled in the catalytic reaction vessel in the oxide state, and hydrogen gas may be circulated and reduced before the reverse shift reaction to be changed to the metallic state. ..
  • the reverse shift catalyst 34 preferably further contains an oxide containing at least one element selected from Si, Al, Zr, and Ce as a carrier component in addition to the active ingredient.
  • oxides containing Ce in particular promote redox. Therefore, from the viewpoint of promoting the oxidation and reduction of the active ingredient and improving the catalytic performance, the carrier component preferably contains an oxide containing Ce.
  • the carrier component is an oxide containing Ce and an oxide containing rare earth elements such as Zr, Y, La, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Tb and Lu. Is more preferable.
  • the combination of the oxide containing Ce and the oxide containing a rare earth element can further promote the redox reaction.
  • the active ingredient is preferably 0.1% by mass or more, more preferably 1% by mass or more, and the upper limit thereof is preferably 30% by mass or less, based on the carrier component. More preferably, it is 10% by mass or less.
  • the reaction temperature is, for example, 550 ° C. or lower, preferably 500 ° C. or lower, and the lower limit thereof is, for example, 200 ° C. or higher, preferably 300 ° C. or higher.
  • the reaction pressure is, for example, 800 hPa or more, preferably 900 hPa or more, and the upper limit thereof is, for example, 1200 hPa or less, preferably 1100 hPa or less.
  • the reverse shift catalyst 34 was prepared, and the catalytic activity of the reverse shift catalyst 34 was evaluated.
  • the specific surface area 100 m 2 / g or more powdered CeO 2 10 g, and the nitrate Cu aqueous solution was impregnated and dried so as to be 10% by mass with respect to CeO 2 by weight of metal Cu terms.
  • a reduction treatment was carried out at 500 ° C. for 1 hour in a hydrogen atmosphere.
  • the production rates were 5%, 25%, and 50%, respectively, and it was found that carbon monoxide was produced from carbon dioxide by using the reverse shift catalyst 34.
  • reaction conditions such as reaction temperature and reaction pressure differ depending on the catalyst used in the reaction that produces carbon monoxide. Therefore, the reaction conditions may be appropriately determined depending on the type of catalyst used.
  • the adsorbent 35 is an example of a water removing mechanism 36 that removes water generated together with carbon monoxide, and in the illustrated example, the adsorbent 35 adsorbs the generated water. Therefore, the carbon monoxide production apparatus 3 includes a water removing mechanism 36, and the water removing mechanism 36 is an adsorbent 35 in the illustrated example.
  • the water removal mechanism 36 By providing the water removal mechanism 36, the chemical equilibrium in the reaction formula (1) can be moved to the right and the amount of carbon monoxide produced can be increased.
  • water in the reaction system can be removed by adsorbing water by the adsorbent 35.
  • the adsorbent 35 preferably contains an oxide containing at least one element selected from, for example, Si and Al, and more preferably contains a zeolite containing Si and Al.
  • the reverse shift catalyst 34 and the adsorbent 35 are housed inside a cylindrical housing 33 having both ends open.
  • the first raw material gas passes through the gap between the reverse shift catalyst 34 and the adsorbent 35 inside the housing 33 toward the opening 33b on the other end side. It flows.
  • carbon dioxide and hydrogen in the first raw material gas react on the surface of the reverse shift catalyst 34 to generate carbon monoxide and water as in the above reaction formula (1).
  • the produced carbon monoxide is taken out as a carbon monoxide-containing gas together with unreacted carbon dioxide and hydrogen through the opening 33b on the other side.
  • the generated water is adsorbed on the adsorbent 35.
  • the adsorption of water to the adsorbent 35 is continued, the amount of water adsorbed is saturated and the water cannot be removed. As a result, it becomes difficult for the chemical equilibrium in the above reaction formula (1) to move to the right, and the carbon monoxide production rate decreases. Therefore, for example, when the production rate of carbon monoxide becomes equal to or lower than a predetermined production rate, the adsorbent 35 is regenerated. As a result, water is separated from the adsorbent 35, and the adsorbent 35 can adsorb water again.
  • Regeneration of the adsorbent 35 is performed using the decompression device 32. Specifically, after the distribution of the first raw material gas to the reaction device 31 is stopped, the inside of the reaction device 31 is sealed by closing a valve (not shown) connected to the openings 33a and 33b. In this state, the inside of the reaction device 31 is depressurized by driving the decompression device 32 that communicates with the inside of the reaction device 31. As a result, water is separated from the adsorbent 35 and taken out of the reactor 31. After sufficiently desorbing water, the first raw material gas is circulated to the reactor 31 again to produce carbon monoxide.
  • the water removing mechanism 36 for removing water generated together with carbon monoxide may be a separation membrane that separates the generated water from the reverse shift catalyst 34.
  • the separation membrane is, for example, a membrane made of zeolite.
  • the separation membrane may be used in place of the above-mentioned adsorbent 35, or may be used together with the adsorbent 35. That is, the water removing mechanism 36 is preferably at least one of the above-mentioned adsorbent 35 and the separation membrane.
  • the compression device 4 compresses the carbon monoxide-containing gas obtained by the carbon monoxide production device 3.
  • the compression device 4 is supplied to the carbon monoxide production device 3 by the carbon monoxide-containing gas system 22. Since the reaction proceeds at, for example, 550 ° C. or lower in the carbon monoxide production apparatus 3, the temperature of the carbon monoxide-containing gas discharged from the carbon monoxide production apparatus 3 is lowered to some extent. Therefore, the load on the compression device 4 to which the carbon monoxide-containing gas is supplied can be reduced. Hydrogen is appropriately supplied to the carbon monoxide-containing gas supplied to the compression device 4.
  • the methanol production apparatus 5 produces methanol using a carbon monoxide-containing gas containing carbon monoxide produced by the carbon monoxide production apparatus 3.
  • the methanol production apparatus 5 is connected to the compression apparatus 4 by the carbon monoxide-containing gas system 22.
  • the carbon monoxide-containing gas is heated as needed.
  • the produced methanol is taken out as a produced gas together with unreacted carbon monoxide, carbon dioxide and hydrogen.
  • the methanol production apparatus 5 includes a methanol production catalyst (not shown) in the illustrated example, and the following reaction formula (2), which is an exothermic reaction, proceeds. CO + 2H 2 ⁇ CH 3 OH... Reaction equation (2)
  • a catalyst composed of copper oxide-zinc oxide-alumina can be used as the methanol production catalyst.
  • the reaction conditions are not particularly limited, but when a methanol catalyst composed of copper oxide-zinc oxide-alumina is used, the temperature can be, for example, 150 ° C. or higher and 350 ° C. or lower, 5 MPa or higher and 15 MPa or lower.
  • the produced gas obtained by the methanol production apparatus 5 is supplied to the first heat exchanger 2 through the first produced gas system 23.
  • the methanol production reaction generated in the methanol production apparatus 5 is an exothermic reaction, and the produced gas discharged from the methanol production apparatus 5 has heat.
  • the carbon monoxide production reaction generated in the carbon monoxide production apparatus 3 is an endothermic reaction, it is preferable that the temperature of the first raw material gas supplied to the carbon monoxide production apparatus 3 is high. Therefore, in the methanol production system 100, the first heat exchanger 2 is installed in the front stage in the flow direction of the first raw material gas of the carbon monoxide production apparatus 3, and the temperature of the first raw material gas is raised by using the heat of the generated gas. NS. As a result, the heat of the generated gas discharged from the methanol production apparatus 5 can be effectively utilized, and the thermal efficiency of the methanol production system 100 can be improved.
  • the methanol recovery device 6 condenses and recovers the methanol in the produced gas by cooling the produced gas after heat transfer to the first raw material gas in the first heat exchanger 2.
  • the methanol recovery device 6 After providing the methanol recovery device 6 after the first heat exchanger 2, the amount of heat lost in the methanol production system 100 can be reduced by cooling the generated gas whose temperature has dropped due to the heat exchange in the first heat exchanger 2. .. Thereby, the thermal efficiency of the entire methanol production system 100 can be improved.
  • the methanol recovery device 6 is connected to the first heat exchanger 2 by the first production gas system 23.
  • the methanol recovery device 6 is, for example, a gas-liquid separator equipped with a cooler, and methanol is recovered as a liquid.
  • the recovered methanol can be used as a liquid fuel, a solvent, or the like.
  • other components in the generated gas that did not condense are discharged as residual gas.
  • Other components in the produced gas that did not condense are, for example, carbon monoxide, carbon dioxide, hydrogen, and the like.
  • FIG. 3 is a flowchart showing the methanol production method of the first embodiment (hereinafter, simply referred to as the production method of the first embodiment).
  • the production method of the first embodiment can be carried out in the methanol production system 100 shown in FIG. 1 above. Therefore, the manufacturing method of the first embodiment will be described with reference to FIG. 1 as appropriate.
  • the production method of the first embodiment includes carbon monoxide production step S1, methanol production step S2, and first heat exchange step S3.
  • the carbon monoxide production step S1, the methanol production step S2, and the first heat exchange step S3 are not performed individually but simultaneously, but for convenience of explanation and illustration. Therefore, each step is shown in order.
  • the carbon monoxide production step S1 is to produce carbon monoxide from the first raw material gas containing carbon dioxide.
  • the carbon monoxide production step S1 is performed by the carbon monoxide production apparatus 3.
  • the reaction conditions in the carbon monoxide production step S1 the contents described in the carbon monoxide production apparatus 3 can be applied.
  • Methanol production step S2 produces methanol using the carbon monoxide-containing gas containing carbon monoxide produced in the carbon monoxide production step S1.
  • the methanol production step S2 is performed by the methanol production apparatus 5.
  • the reaction conditions in the methanol production step S2 the contents described in the methanol production apparatus 5 can be applied.
  • the first heat exchange step S3 transfers the heat of the generated gas containing methanol produced in the methanol production step S2 to the first raw material gas.
  • the first heat exchange step S3 is performed by the first heat exchanger 2.
  • the heat generated in the exothermic reaction of methanol production can be used for the endothermic reaction of carbon monoxide production.
  • the amount of heat lost as a whole can be reduced and the thermal efficiency can be improved.
  • FIG. 4 is a system diagram showing the methanol production system 200 of the second embodiment.
  • the methanol production system 200 includes a merging system 25, a second heat exchanger 7, and a second production gas system 24, in addition to the configuration of the methanol production system 100 (FIG. 1).
  • the merging system 25 merges the residual gas after methanol recovery by the methanol recovery device 6 with the carbon monoxide-containing gas obtained by the carbon monoxide production device 3.
  • methanol can be produced by the methanol production apparatus 5 by using the unreacted components in the residual gas together with the carbon monoxide-containing gas.
  • the second heat exchanger 7 transfers the heat of the generated gas to the carbon monoxide-containing gas.
  • the second heat exchanger 7 is connected to each of the methanol production device 5 and the methanol recovery device 6 by the second production gas system 24.
  • the merging system 25 is connected to the upstream side of the second heat exchanger 7 in the flow direction of carbon monoxide gas.
  • the temperature of the carbon monoxide-containing gas decreases due to the confluence of the residual gas whose temperature has decreased due to cooling in the methanol recovery device 6. Therefore, the carbon monoxide-containing gas whose temperature has decreased can be raised by the second heat exchanger 7, and the raised carbon monoxide-containing gas can be supplied to the methanol production apparatus 5. As a result, the reaction using the carbon monoxide-containing gas in the methanol production apparatus 5 can be stabilized. At this time, the carbon monoxide-containing gas after merging may be supplementarily heated if necessary.
  • the flow rate ratio of the flow rate of the produced gas flowing through the first produced gas system 23 to the flow rate of the produced gas flowing through the second produced gas system 24 depends on, for example, the temperature of the produced gas, the residual gas, the carbon monoxide-containing gas, or the like. Can be changed as appropriate. Although not shown, the flow rate ratio can be changed by adjusting the opening degree of the valve provided in the first generated gas system 23 and the valve provided in the second generated gas system 24, for example.
  • FIG. 5 is a system diagram showing the methanol production system 300 of the third embodiment.
  • the methanol production system 300 includes a merging system 25, a third heat exchanger 8, and a third production gas system 26 in addition to the configuration of the methanol production system 100 (FIG. 1).
  • the third heat exchanger 8 transfers the heat of the produced gas obtained by the methanol production apparatus 5 to the residual gas after the methanol recovery by the methanol recovery apparatus 6.
  • the third heat exchanger 8 is connected to each of the methanol production device 5 and the methanol recovery device 6 by the third production gas system 26.
  • the residual gas may be supplementarily heated if necessary.
  • the temperature drop of the carbon monoxide-containing gas can be suppressed.
  • the carbon monoxide-containing gas after the residual gas merge can be supplied to the methanol production apparatus 5 as it is.
  • FIG. 6 is a system diagram showing the methanol production system 400 of the fourth embodiment.
  • the methanol production system 400 includes a carbon dioxide recovery device 9, a fourth production gas system 27, and a second raw material gas system 28, in addition to the configuration of the methanol production system 100 (FIG. 1).
  • the carbon dioxide recovery device 9 recovers carbon dioxide used for the first raw material gas from the second raw material gas containing carbon dioxide.
  • the carbon dioxide capture device 9 will be described with reference to FIG. 7.
  • FIG. 7 is a schematic view showing the carbon dioxide capture device 9.
  • the carbon dioxide recovery device 9 includes a recovery device 91, a desorption device 92, and a fourth heat exchanger 93.
  • the recovery device 91 recovers carbon dioxide into an alkaline aqueous solution by contacting a second raw material gas containing carbon dioxide with an alkaline aqueous solution. Carbon dioxide is absorbed by the alkaline aqueous solution by contact with the alkaline aqueous solution.
  • the second raw material gas is supplied to the recovery device 91 through the second raw material gas system 28.
  • the second raw material gas is, for example, combustion exhaust gas in a thermal power plant or the like.
  • the alkaline aqueous solution is, for example, an ammonia aqueous solution, an amine aqueous solution, or the like.
  • the recovery device 91 is, for example, an absorption tower.
  • the second raw material gas rises inside the absorption tower.
  • the carbon dioxide in the second raw material gas is absorbed by the alkaline aqueous solution.
  • the gas remaining after the absorption of carbon dioxide is discharged from the top of the absorption tower as off-gas.
  • the alkaline aqueous solution from which carbon dioxide has been recovered is supplied from the recovery device 91 to the desorption device 92 through the alkaline aqueous solution system 29.
  • the desorption device 92 uses the heat of the produced gas obtained in the methanol production device 5 (FIG. 6) to desorb carbon dioxide by heating an alkaline aqueous solution in which carbon dioxide is recovered.
  • the detachment device 92 is, for example, a regeneration tower.
  • the fourth heat exchanger 93 generates steam by transferring the heat of the produced gas supplied through the fourth produced gas system 27 to the water flowing through the heat medium system 30. Therefore, the desorption device 92 desorbs carbon dioxide by using the heat of the generated gas supplied through the fourth heat exchanger 93.
  • the fourth heat exchanger 93 is, for example, a reboiler.
  • the alkaline aqueous solution in which carbon dioxide is recovered is supplied from the recovery device 91 to the desorption device 92 through the alkaline aqueous solution system 29.
  • This alkaline aqueous solution is sprinkled inside the desorption device 92.
  • steam is generated by transferring the heat of the generated gas to the water extracted from the desorption device 92 through the heat medium system 30.
  • the generated steam is supplied to the desorption device 92 through the heat medium system 30, and is discharged into the desorption device 92 below the watering portion of the alkaline aqueous solution.
  • the alkaline aqueous solution sprinkled by the release of steam is heated, and carbon dioxide is desorbed from the alkaline aqueous solution.
  • the desorbed carbon dioxide is extracted from the top of the regeneration tower and merges with hydrogen to obtain the first raw material gas.
  • the alkaline aqueous solution after carbon dioxide desorption accumulates in the lower part of the regeneration tower.
  • a part of the accumulated alkaline aqueous solution is extracted through the heat medium system 30 and heated by the fourth heat exchanger 93. Further, another part of the accumulated alkaline aqueous solution is extracted through the alkaline aqueous solution system 29 and returned to the recovery device 91.
  • the carbon dioxide contained in the first raw material gas includes the carbon dioxide recovered by the carbon dioxide recovery device 9.
  • carbon dioxide used for producing carbon monoxide can be recovered from the second raw material gas by utilizing the heat of the produced gas obtained by the methanol producing apparatus 5.
  • the heat of the generated gas was used to change the liquid water into steam, but the heat of the generated gas is, for example, another heat exchanger (for example, illustrated). It may be used to further raise the temperature of the steam produced using the non-reboiler).

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  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un système de production de méthanol capable d'améliorer l'efficacité thermique. Ce système de production de méthanol (100) est caractérisé en ce qu'il comprend un dispositif de production de monoxyde de carbone (3) qui produit du monoxyde de carbone à partir d'un premier gaz d'alimentation, qui comprend du dioxyde de carbone, un dispositif de production de méthanol (5) qui produit du méthanol à partir d'un gaz contenant du monoxyde de carbone produit par le dispositif de production de monoxyde de carbone (3), et un premier échangeur de chaleur (2), qui conduit la chaleur possédée par un gaz produit contenant du méthanol produit par le dispositif de production de méthanol (5), vers le premier gaz d'alimentation.
PCT/JP2020/012205 2020-03-19 2020-03-19 Système de production de méthanol et procédé de production de méthanol WO2021186658A1 (fr)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023162696A1 (fr) * 2022-02-25 2023-08-31 Ｅｎｅｏｓ株式会社 Dispositif et procédé de production d'hydrocarbures
WO2024004464A1 (fr) * 2022-06-30 2024-01-04 三菱瓦斯化学株式会社 Procédé et dispositif de production de méthanol

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JPH08176034A (ja) * 1994-12-22 1996-07-09 Cosmo Sogo Kenkyusho:Kk メタノールの合成方法
JP2002226870A (ja) * 2001-01-29 2002-08-14 Takeshi Hatanaka メタノールの製造法およびその装置
WO2016152698A1 (fr) * 2015-03-20 2016-09-29 積水化学工業株式会社 Procédé et dispositif de production d'une substance organique
WO2019116484A1 (fr) * 2017-12-14 2019-06-20 三菱重工エンジニアリング株式会社 Installation de co-production d'oléfine et de méthanol, et procédé de co-production d'oléfine et de méthanol

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Publication number Priority date Publication date Assignee Title
US4235799A (en) * 1979-04-16 1980-11-25 Stiles Alvin B Production of methanol
JPH0852304A (ja) * 1994-07-06 1996-02-27 Rhone Poulenc Chim ガス状或は液状混合物をアルミナ及びモレキュラーシーブで構成される吸着装置を使用して乾燥させる方法
JPH08176034A (ja) * 1994-12-22 1996-07-09 Cosmo Sogo Kenkyusho:Kk メタノールの合成方法
JP2002226870A (ja) * 2001-01-29 2002-08-14 Takeshi Hatanaka メタノールの製造法およびその装置
WO2016152698A1 (fr) * 2015-03-20 2016-09-29 積水化学工業株式会社 Procédé et dispositif de production d'une substance organique
WO2019116484A1 (fr) * 2017-12-14 2019-06-20 三菱重工エンジニアリング株式会社 Installation de co-production d'oléfine et de méthanol, et procédé de co-production d'oléfine et de méthanol

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023162696A1 (fr) * 2022-02-25 2023-08-31 Ｅｎｅｏｓ株式会社 Dispositif et procédé de production d'hydrocarbures
WO2024004464A1 (fr) * 2022-06-30 2024-01-04 三菱瓦斯化学株式会社 Procédé et dispositif de production de méthanol

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