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    • 专利摘要:

    公开号:BE1020423A5
    申请号:E2011/0402
    申请日:2011-06-29
    公开日:2013-10-01
    发明作者:Motonobu Yoshikawa；Takehiro Nakasuji
    申请人:Sumitomo Chemical Co；
    IPC主号:
    专利说明:

    PROCESS FOR THE PRODUCTION OF METHIONINE Background of the Invention 1. Field of the Invention
    The present invention relates to a process for producing methionine using carbon dioxide which is separated and recovered from a burnt combustion gas obtained by pure oxygen combustion.
    2. Description of the prior art
    A process for the production of methionine is known by reacting 3-methylthiopropanal as a raw material with hydrocyanic acid in the presence of a base, subsequent reaction of the resulting product with ammonium carbonate and subsequent hydrolysis of the reaction product. . Carbon dioxide is introduced into this process in the reaction liquid after the hydrolysis, at which time crystallization takes place and separate methionine can be obtained in the form of a crystal.
    The carbon dioxide to be introduced into the reaction liquid after the hydrolysis comprises carbon dioxide which is produced in a process for producing hydrogen by a steam reforming reaction, and carbon dioxide which is obtained by rinsing and purifying a flue gas produced by a boiler or the like. Hydrogen is also used as feedstock for the production of methionine, and thus the steam reforming reaction is generally used since a reformed gas containing hydrogen and carbon dioxide is thereby produced.
    The molar ratio of hydrogen and carbon dioxide for the production of methionine is hydrogen / carbon dioxide = 1/1. The molar ratio of hydrogen and carbon dioxide produced by the steam reforming reaction is, on the other hand, approximately hydrogen / carbon dioxide = 3/1. Assuming that the hydrogen and carbon dioxide contained in the reformed gas obtained by the steam reforming reaction are used as raw materials for the production of methionine, hydrogen remains, and facilities for treating hydrogen in excess are therefore necessary.
    Japanese Unexamined Patent Application JP-A 2003/81605 discloses a process for producing hydrogen, wherein the hydrogen is separated and purified from a reformed gas obtained by subjecting liquefied natural gas to a reaction. steam reforming, and gaseous effluents containing separated combustible substances in the hydrogen purification process are used for heating combustion in the steam reforming reaction. In the hydrogen production process described in JP-A-2003/81605, pure oxygen or oxygen of high concentration is introduced, which is separated cryogenically using the liquefaction heat of liquefied natural gas. , as an oxidizing agent for the combustion of gaseous effluents during heating for combustion in the steam reforming reaction, and carbon dioxide is separated and recovered at a high concentration from the combustion flue gases produced during combustion . In the process for producing hydrogen, carbon dioxide is obtained in the reformed gas obtained by the steam reforming reaction and the high concentration carbon dioxide, separated and recovered from the flue gases.
    JP-A-2003-81605, however, does not consider the use of hydrogen and carbon dioxide formed and recovered in the production of hydrogen as raw materials for the production of methionine. Hydrogen therefore remains for the production of methionine in which hydrogen and carbon dioxide are used at a molar ratio hydrogen / carbon dioxide = 1/1, and facilities for treating excess hydrogen are still needed.
    Summary of the invention
    An object of the invention is therefore to provide a process for producing methionine using hydrogen and carbon dioxide which is formed and recovered in the production of hydrogen, the process of lowering the amount of excess hydrogen.
    The invention provides a process for producing methionine comprising: a hydantoin forming step comprising obtaining 5- (P-methylmercaptoethyl) hydantoin using hydrogen sulfide obtained by reaction of hydrogen and sulfur; a hydrolysis step comprising hydrolyzing 5- (β-methylmercaptoethyl) hydantoin; a crystallization step comprising crystallization with carbon dioxide introduced into a reaction solution after hydrolysis, to obtain methionine; and a feedstock stage comprising introducing hydrogen and carbon dioxide which are formed and recovered from a hydrogen generating apparatus, wherein a reformed gas is obtained by subjecting a hydrocarbon heated with a hydrocarbon heating furnace and steam to a steam reforming reaction under combustion heating in a heating furnace of the reforming reaction, such as hydrogen for use in the formation step of hydantoin and as carbon dioxide for use in the crystallization step, in the feedstock stage, the hydrogen which is separated and recovered from the reformed gas obtained in the hydrogen production apparatus is introduced for use in the hydantoin-forming step, the carbon dioxide that is separated and recovered from the reformed gas obtained in the apparatus of Hydrogen production is introduced for use in the crystallization step as the main carbon dioxide, and the carbon dioxide that is separated and recovered from a combustion flue gas produced in the combustion in the heating furnace. hydrocarbon for heating the hydrocarbon, and the carbon dioxide which is separated and recovered from a burnt combustion gas produced by the combustion in the heating furnace of the reforming reaction of the steam reforming reaction with oxygen obtained by cryogenic separation of the air introduced as oxidation agent being recycled and introduced into the hydrocarbon heating furnace and the heating furnace of the reforming reaction, are introduced for use in the crystallization step as auxiliary carbon dioxide with oxygen obtained as an oxidizing agent by cryogenic separation of air.
    The process for producing methionine comprises according to the invention: a hydantoin-forming step comprising obtaining 5- (3-methylmercaptoethyl) hydantoin using hydrogen sulphide obtained by the reaction of hydrogen and sulfur ; a hydrolysis step comprising hydrolyzing 5- (p-methylmercaptoethyl) -hydantoin; a crystallization step comprising crystallization with carbon dioxide introduced into a reaction solution after hydrolysis, to obtain methionine; and a step of feeding raw materials.
    In the feedstock step, hydrogen that is separated and recovered from the reformed gas obtained in the hydrogen generating apparatus is introduced for use in the formation step of hydantoin. In the feedstock stage, carbon dioxide which is separated and recovered from the reformed gas obtained in the hydrogen production apparatus is further introduced for use in the crystallization step. as main carbon dioxide, and carbon dioxide that is separated from a combustion flue gas produced during combustion in the heating furnace for heating the hydrocarbon, and carbon dioxide that is separated to from a combusted combustion gas produced by the combustion in the heating furnace of the steam reforming reaction with pure oxygen or high concentration oxygen obtained by cryogenic separation of the air introduced as an agent oxidant (pure oxygen combustion) are introduced for use in the crystallization step as auxiliary carbon dioxide.
    It is further preferred in the method for producing methionine of the invention that the combustion in the heating furnace for heating the hydrocarbon in the hydrogen generating apparatus is a combustion with oxygen obtained by cryogenic separation of the air introduced as an oxidizing agent.
    In addition, in the methionine production process of the invention, the combustion in the heating furnace for heating the hydrocarbon in the hydrogen production apparatus is preferably a combustion with pure oxygen or oxygen. oxygen of high concentration obtained by cryogenic separation of the air introduced as oxidizing agent (pure oxygen combustion).
    It is furthermore preferable in the methionine production process of the invention that steam for use in the steam reforming reaction is produced using the thermal energy of reformed gas from the reforming reaction to the reforming reaction. steam in the apparatus for producing hydrogen.
    Methionine is produced in the methionine production process according to the invention using hydrogen and carbon dioxide obtained from the hydrogen production apparatus at a molar ratio of hydrogen to carbon dioxide = 1. / 1, which consist of hydrogen and carbon dioxide which are separated and recovered from the reformed gas obtained by the steam reforming reaction (carbon dioxide of main material) and carbon dioxide of high concentration which is separated and recovered from the combusted combustion gas by pure oxygen combustion (auxiliary carbon dioxide), and the amount of excess hydrogen can therefore be lowered.
    Steam for use in the steam reforming reaction is produced in the methionine production process using the thermal energy of the reformed gas of the steam reforming reaction. Therefore, in the case of obtaining hydrogen and carbon dioxide at a hydrogen / carbon dioxide molar ratio = 1/1 in the hydrogen production apparatus, the thermal energy in excess of the amount that is needed for the steam reforming reaction can be recovered as steam.
    Brief description of the drawings
    Additional and additional objects, aspects and advantages of the invention will become more explicit from the following detailed description made in connection with the drawings in which: FIG. 1 is a diagram showing a configuration of a hydrogen generating apparatus which produces carbon dioxide and hydrogen, used in a method of producing methionine according to one embodiment of the invention.
    detailed description
    Now described below with reference to the drawings of the preferred embodiments of the invention.
    The methionine production method of the invention is a process for producing methionine using hydrogen and carbon dioxide which are formed and recovered in the production of hydrogen, and the method comprises a hydantoin formation step , a hydrolysis step and a crystallization step. The hydantoin formation step comprises a hydrogen sulfide forming step, a methyl mercaptan forming step, an acrolein forming step, a methyl thiopropanal forming step, a cyanohydrin forming step, and a step of hydantoin formation.
    In the hydrogen sulfide forming step, hydrogen sulfide (H2S) is obtained by reacting hydrogen (H2) and sulfur (S) as shown in the following equation (1). Hydrogen is used in the hydrogen sulfide formation step.
    H2 "H S -H2S * * * (1)
    In the methyl mercaptan forming step, methyl mercaptan (CH 3 SH) is obtained by the reactions shown in the following equations (2), (3) and (4). CH3OH represents methanol and CH3SCH3 represents dimethylsulfide in equations (2), (3) and (4).
    H2s -f CH3OH-CHCHgSH + HzO --- (2) CH3OH + CH3SH-CHCH3SCH3 + H20 --- (3) CH3SCH3 -fH2S ► 2CH3SH --- (4)
    Acrolein (CH 2 = CHCHO) is obtained in the acrolein formation step by reaction of propylene (CH 2 = CHCH 3) and oxygen (O 2) as shown in the following equation (5).
    ch2 = chch3 + o2-ch2 = chcho + h2o --- (5)
    3-Methylthiopropanal is obtained in the methylthiopropanal formation step by reaction of acrolein and methyl mercaptan as shown in the following equation (6).
    • · · (6)
    2-Hydroxy-4-methylthiobutanenitrile is obtained in the cyanohydrin forming step by reaction of 3-methylthiopropanal and hydrocyanic acid (HCN) as shown in the following equation (7).
    In the hydantoin formation step, 5- (β-methylmercaptoethyl) hydantoin is obtained by reaction of 2-hydroxy-4-methylthiobutanenitrile and ammonium carbonate as shown in the following equation (8). Hydantoin can be used in the hydantoin forming step as it is or can be used in the form of an aqueous solution of ammonium carbonate. The ammonium carbonate may be further prepared from gaseous carbon dioxide and ammonia in the reaction system or solvent, or ammonium carbonate prepared from ammonium bicarbonate and potassium hydroxide.
    5- (p-Methylmercaptoethyl) hydantoin is hydrolysed in the hydrolysis step in the presence of a basic potassium compound, thereby obtaining methionine, as shown in the following equation (9). Examples of the basic potassium compound include potassium hydroxide, potassium carbonate and potassium hydrogencarbonate, of which two or more types may be used as needed. The hydrolysis reaction can be carried out in water and the methionine is present as a potassium salt in the resulting hydrolysis reaction solution.
    • "(9)
    Crystallization is carried out in the crystallization stage with carbon dioxide introduced into the reaction solution, for the collection of methionine present in the form of a potassium salt in the hydrolysis reaction solution, and the resulting suspension is separated into a deposition product and a mother liquor by filtration, decantation or equivalent, thereby obtaining methionine in the form of crystals. The reaction solution absorbs carbon dioxide upon introduction of carbon dioxide, and free methionine is deposited from the potassium salt of methionine. Carbon dioxide is used in the crystallization step.
    The thus separated methionine can be rinsed, pH adjusted and the like if necessary, and can then be dried to provide the product.
    The methionine is produced in the method of producing methionine according to the embodiment using hydrogen and carbon dioxide formed and recovered in the production of hydrogen.
    Fig. 1 is a diagram showing a configuration of a hydrogen generating apparatus which produces carbon dioxide and hydrogen, used in the method of producing methionine according to the embodiment of the invention. The hydrogen generating apparatus produces hydrogen by performing a steam reforming reaction with a hydrocarbon and steam as raw materials. The step of feeding raw materials is carried out in the process for producing methionine according to the embodiment with the hydrogen production apparatus 20.
    Examples of the hydrocarbon include natural gas containing methane as the main constituent, liquefied petroleum gas (LPG), liquefied natural gas (LNG) and naphtha, and LPG is used in the embodiment. The hydrocarbon preferably has a low sulfur concentration to reduce pollution in the crystallization step.
    The hydrogen production apparatus 20 comprises a cryogenic air separation section 10, a hydrocarbon heating section 11 comprising a hydrocarbon heater 111 and a hydrocarbon heating furnace 112, a hydrogenation and desulfurization section 12, a steam reforming section 13 comprising a reforming reactor 131 and a heating furnace for the reforming reaction 132, a carbon monoxide modification section 14, a separation section of carbon dioxide 15, a purification section 16 and a flue gas separation section 17.
    The cryogenic separation section of air 10 subjects air as a raw material to cryogenic separation to form pure oxygen or high concentration oxygen. The oxygen which is obtained by the cryogenic separation of the air (which may be hereafter referred to as "oxygen from the cryogenic separation of air") is introduced into the hydrocarbon heating furnace 112 of the heating the hydrocarbon 11 and in the heating furnace for the reforming reaction 132 of the steam reforming section 13, and is used as an oxidizing agent for a heating combustion.
    The hydrocarbon heating section 11 comprises the hydrocarbon heater 111 and the hydrocarbon heating furnace 112 and heats the LPG as the feedstock of the steam reforming reaction (which may be hereinafter referred to as "LPG reaction material"). The LPG reaction material is introduced into the hydrocarbon heater 111 and the LPG reaction material thus introduced is heated, for example, to 620 ° C with the combustion heat energy in the hydrocarbon heating furnace 112. The The LPG reaction material thus heated is introduced into the hydrogenation and desulfurization section 12.
    LPG as a combustion fuel (which may be hereinafter referred to as "LPG combustion fuel"), the oxygen of the cryogenic separation of air as an oxidizing agent from the cryogenic separation section of air 10, and carbon dioxide as a diluent from the flue gas separation section 17 (which may hereinafter be referred to as "recycled carbon dioxide") is introduced into the hydrocarbon heating furnace 112. The LPG combustion fuel is introduced into the hydrocarbon heating furnace 112 for example at 67.4 kg / h (1.16 kmol / h), the oxygen of the cryogenic separation of the air is introduced at 180 Nm3 / h, and the Recycled carbon dioxide (temperature: 225 ° C) is introduced at 635 Nm3 / h, thereby achieving combustion with oxygen from the cryogenic separation of the air introduced as an oxidizing agent (pure oxygen combustion). Combustible flue gas is produced by pure oxygen combustion and carbon dioxide is produced at 4.6 kmol / h (104 Nm3 / h) as a component of the flue gas. The combusted combustion gas produced from the hydrocarbon heating furnace 112 is introduced into the flue gas separation section 17.
    The hydrogenation and desulfurization section 12 subjects the LPG reaction material, which has been heated in the hydrocarbon heating section 11, to hydrogenation and desulfurization. The LPG reaction material having been subjected to hydrogenation and desulfurization is introduced into the reforming reactor 131 of the steam reforming section 13.
    The steam reforming section 13 comprises the reforming reactor 131 and the heating furnace of the reforming reaction 132 and performs a steam reforming reaction. The reforming reactor 131 performs a steam reforming reaction with the LPG reaction material introduced from the hydrogenation and desulfurization section 12 and with steam as raw materials. The steam reforming reaction carried out in the reforming reactor 131 is carried out in the presence of a reforming catalyst, such as a catalyst of the Ni (nickel) series or of the Ru (ruthenium) series, in the heating furnace of the reforming reaction 132 at an elevated temperature of 500 ° C to 1000 ° C, preferably 800 ° C to 1000 ° C (which is 850 ° C in the embodiment), in a high pressure of approximately 0.5 MPa to 3.5 MPa. When the temperature of the steam reforming reaction exceeds 1000 ° C, an aromatic hydrocarbon is disadvantageously formed adjacent to the wall of the reforming reactor 131.
    In the reforming reactor 131, the realized steam reforming reaction produces a reformed gas containing hydrogen, carbon monoxide, and carbon dioxide as the gases produced, and hydrocarbon and steam as a gas. having not reacted. The reformed gas in the reforming reaction 131 is introduced into the carbon monoxide modification section 14.
    In the reforming reactor 131, for example, the LPG reaction material is introduced at 58.5 kmol / h, thereby achieving the steam reforming reaction. The steam reforming reaction produces a reformed gas, and hydrogen is produced at 760.5 kmol / h, and carbon dioxide is produced at 234.0 kmol / h as reformed gas components.
    In addition, in the method of producing methionine according to the embodiment, steam for use in the steam reforming reaction is produced using the thermal energy of the reformed gas of the steam reforming reaction. in the reforming reactor 131. Therefore, in the case of obtaining hydrogen and carbon dioxide at a molar ratio of hydrogen / carbon dioxide = 1/1 in the hydrogen production apparatus 20, it is may recover as heat vapor excess heat energy from the amount required for the steam reforming reaction.
    LPG combustion fuel, oxygen from the cryogenic separation of air as an oxidizing agent from the cryogenic separation section of air 10, recycled carbon dioxide as a diluent from the flue gas separation section and gaseous effluents (which contain hydrogen, methane, carbon monoxide, carbon dioxide and the like) from the purification section 16 are introduced into the heating furnace of the reforming reaction 132. heating furnace of the reforming reaction 132, LPG combustion fuel is for example introduced at 4 123 kg / h (70.93 mmol / h), the oxygen of the cryogenic separation of the air is introduced at 12 252 Nm3 / h, the recycled carbon dioxide (temperature: 225 ° C) is introduced at 113 560 Nm3 / h and the gaseous effluents are introduced at 3700 Nm3 / h, thereby achieving a combustion with oxygen from the separation cryogenic air introduced comm e oxidizing agent (pure oxygen combustion). Combustible flue gas is produced by pure oxygen combustion and carbon dioxide is produced at 356.4 kmol / h (7,983 Nm3 / h) as a constituent of the flue gas. The flue gas produced from the heating furnace of the reforming reaction 132 is introduced into the flue gas separation section 17.
    The carbon monoxide modification section 14 converts the carbon monoxide contained in the reformed gas introduced from the reforming reactor 131 into carbon dioxide. The carbon monoxide modification section 14 includes a high temperature modification section and a low temperature modification section. In the high temperature modification section, the conversion reaction is carried out in the presence of an iron oxide and chromium catalyst to lower the carbon monoxide concentration in the reformed gas, and in the low temperature modification section, the conversion reaction is carried out in the presence of a copper oxide-zinc catalyst to further lower the carbon monoxide concentration in the reformed gas. A heat exchanger which carries out the heat exchange is disposed between the high temperature modification section and the low temperature modification section. The reformed gas discharged from the carbon monoxide modification section 14 is introduced into the carbon dioxide separation section 15.
    The carbon dioxide separation section 15 separates and recovers the carbon dioxide from the reformed gas introduced from the carbon monoxide modification section 14. The carbon dioxide thus separated and recovered by the carbon dioxide separation section It is introduced into the hydrolysis reaction solution as the main carbon dioxide for use in the crystallization step.
    The reformed gas is produced by the steam reforming reaction in the reforming reactor 131, and carbon dioxide is produced as a constituent of the reformed gas at 234.0 kmol / h, as described above. The carbon dioxide separation section 15 separates and recovers carbon dioxide from the reformed gas. The carbon dioxide separation section 15 specifically separates and recovers carbon dioxide at 171.3 kmol / h (3,837 Nm 3 / h) from the reformed gas. The reformed gas discharged from the carbon dioxide separation section 15 is introduced into the purification section 16.
    The purification section 16 separates and recovers hydrogen from the reformed gas introduced from the carbon dioxide separation section 15. The hydrogen thus separated and recovered by the purification section 16 is introduced as hydrogen for use in the reactor. Hydrogen sulfide formation step of the hydantoin formation step.
    The purification section 16 may have a structure in which hydrogen is separated with an adsorbent by pressure modulation adsorption or temperature modulated adsorption, or a structure using a hydrogen separation membrane that selectively transmits only hydrogen. The purification section 16 has in the embodiment a structure in which hydrogen is separated by pressure swing adsorption (PSA). The reformed gas is produced by the steam reforming reaction in the reforming reactor 131, and hydrogen is produced as a component of the reformed gas at 760.5 kmol / h, as described above. The purification section 16 separates and recovers hydrogen from the reformed gas. The purification section 16 separates and recovers the hydrogen specifically at 532.3 kmol / h (11,924 Nm3 / h) from the reformed gas.
    The burnt gas separation section 17 separates and recovers the carbon dioxide from the combustion burned gas produced by the pure oxygen combustion, which is introduced from the hydrocarbon heating furnace 112 and the heating furnace of the Reforming reaction 132. Carbon dioxide thus separated and recovered by the flue gas separation section 17 is introduced into the hydrolysis reaction solution, as auxiliary carbon dioxide for use in the crystallization step.
    Combustion flue gas is produced by pure oxygen combustion in the hydrocarbon heating furnace 112 and carbon dioxide is produced at 4.6 kmol / hr (104 Nm3 / hr) as a component of the flue gas of combustion, as described above. The combusted combustion gas is produced by pure oxygen combustion in the heating furnace of the reforming reaction 132, and carbon dioxide is produced at 356.4 kmol / h (7,983 Nm 3 / h) as a burned gas component as described above. The flue gas separation section 17 separates and recovers carbon dioxide from the combustion flue gas produced by pure oxygen combustion in the hydrocarbon heating furnace 112 and in the heating furnace of the reforming reaction 132. The burnt gas separation section 17 specifically separates and recovers carbon dioxide at 361.0 kmol / h (8,087 Nm3 / h) from the combusted combustion gas in the hydrocarbon heating furnace 112 and in the heating furnace of the reforming reaction 132.
    In the hydrogen production apparatus having the above-mentioned structure, the LPG feedstock feed amount for use in the steam reforming reaction in the reforming reactor 131, and the amounts supplying LPG combustion fuel, oxygen from the cryogenic separation of air, recycled carbon dioxide and gaseous effluents for use in pure oxygen combustion in the hydrocarbon heating furnace 112 and in the heating furnace of the reforming reaction 132 are adjusted so that the amount of hydrogen recovered in the purification section 16 (532.3 kmol / h) and the total amount of carbon dioxide recovered in the section of carbon dioxide separation and in the flue gas separation section 17 (171.3 + 361.0 = 532.3 kmol / h) have a hydrogen / carbon dioxide molar ratio = 1/1.
    In the crystallization step of the methionine production process according to the embodiment, carbon dioxide introduced into the hydrolysis reaction solution is used as carbon dioxide which is separated in the carbon dioxide separation section. from the reformed gas obtained by the steam reforming reaction in the steam reforming section 13 (main material carbon dioxide), and carbon dioxide which is separated in the flue gas separation section 17 from combustion flue gas produced by the pure oxygen combustion with oxygen of the cryogenic separation of the air obtained in the cryogenic separation section of the air 10 introduced as an oxidizing agent into the heating furnace of hydrocarbon 112 and in the heating furnace of the reforming reaction 132 (auxiliary carbon dioxide).
    Methionine is produced in the method of producing methionine according to the present embodiment using hydrogen and carbon dioxide obtained from the hydrogen generating apparatus at a hydrogen / carbon dioxide molar ratio. carbon = 1/1, which consist of hydrogen and carbon dioxide that are formed by the steam reforming reaction (main carbon dioxide) and carbon dioxide of high concentration which is separated and recovered from the burned combustion gas by burning with pure oxygen (auxiliary carbon dioxide), and the amount of excess hydrogen can therefore be lowered.
    The invention may be embodied in other specific forms without departing from its spirit or essential characteristics. The present embodiments should therefore be considered in all respects as illustrative and not restrictive and any modifications within the scope of the present invention without departing from its spirit are therefore a part thereof.
    权利要求:
    Claims (3)
    [1]
    A process for producing methionine, characterized in that it comprises: a hydantoin-forming step comprising obtaining 5- (p-methylmercaptoethyl) hydantoin using hydrogen sulfide obtained by reaction of hydrogen and sulfur; a hydrolysis step comprising hydrolyzing 5- (β-methylmercaptoethyl) hydantoin; a crystallization step comprising crystallization with carbon dioxide introduced into a reaction solution after hydrolysis, to obtain methionine; and a feedstock stage comprising introducing hydrogen and carbon dioxide which are formed and recovered from a hydrogen generating apparatus (20), wherein a reformed gas is obtained from subjecting a hydrocarbon heated with a hydrocarbon heating furnace (112) and steam to a steam reforming reaction under combustion heating in a heating furnace of the reforming reaction (132), as hydrogen to be used in the hydantoin-forming step and as carbon dioxide for use in the crystallization step, in the feedstock step, the hydrogen which is separated and recovered from the reformed gas obtained in the hydrogen generating apparatus (20) is introduced for use in the hydantoin forming step, the carbon dioxide which is separated and recovered from the ref gas orme obtained in the hydrogen production apparatus (20) is introduced for use in the crystallization step as the main carbon dioxide, and the carbon dioxide that is separated and recovered from a burned gas of combustion produced by combustion in the hydrocarbon heating furnace (112) for heating the hydrocarbon, and the carbon dioxide that is separated and recovered from a combustion flue gas produced by combustion in the heating furnace of the reforming reaction (132) of the steam reforming reaction with oxygen obtained by cryogenic separation of the introduced air as oxidizing agent being recycled and introduced into the hydrocarbon heating furnace and into the heating furnace of the reforming reaction, are introduced for use in the crystallization step as auxiliary carbon dioxide with oxygen obtained as an oxidizing agent by cryogenic separation of the air.
    [2]
    Process for the production of methionine according to claim 1, characterized in that the combustion in the heating furnace (112) for heating the hydrocarbon in the hydrogen production apparatus (20) is a combustion with the oxygen obtained by cryogenic separation of the air introduced as an oxidizing agent.
    [3]
    Process for the production of methionine according to claim 1 or 2, characterized in that steam for use in the steam reforming reaction is produced using the thermal energy of the reformed gas from the reforming reaction to the steam in the hydrogen production apparatus (20).
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    申请号 | 申请日 | 专利标题
    JP2010148375|2010-06-29|
    JP2010148375A|JP5524736B2|2010-06-29|2010-06-29|Method for producing methionine|
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