WO2025250041A1 - Procédé de production d'ammoniac et de méthanol à partir de gaz naturel - Google Patents

Procédé de production d'ammoniac et de méthanol à partir de gaz naturel

Info

Publication number
WO2025250041A1
WO2025250041A1 PCT/RU2025/000114 RU2025000114W WO2025250041A1 WO 2025250041 A1 WO2025250041 A1 WO 2025250041A1 RU 2025000114 W RU2025000114 W RU 2025000114W WO 2025250041 A1 WO2025250041 A1 WO 2025250041A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
hydrogen
methanol
pressure
ammonia
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/RU2025/000114
Other languages
English (en)
Russian (ru)
Inventor
Игорь Анатольевич МНУШКИН
Дмитрий Иванович МАЛЬЦЕВ
Линар Ильдусович МИФТАХОВ
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from RU2024114649A external-priority patent/RU2832477C1/ru
Application filed by Individual filed Critical Individual
Publication of WO2025250041A1 publication Critical patent/WO2025250041A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis
    • 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 invention relates to the field of obtaining ammonia and methanol from natural gas and air and can be used in gas chemical industry enterprises.
  • Ammonia is the most important source of raw material for the production of nitrogen fertilizers, mainly urea and ammonium nitrate.
  • the raw materials for ammonia production are nitrogen and hydrogen in a 1:3 ratio.
  • Nitrogen is primarily obtained through energy-intensive low-temperature air rectification, while hydrogen is produced by steam reforming of natural gas (66%), gasification of solid fuels, electrolysis, or thermal decomposition of water.
  • Natural gas can also serve as a feedstock for another large-scale production - methanol production.
  • production of this product in Russia has nearly doubled, reaching over 4 million tons per year.
  • Some of the main consumers of methanol are phenol-formaldehyde resin producers and natural gas production and transportation systems.
  • a method for producing ammonia from natural gas includes compression, heating and purification of natural gas from sulfur compounds, two-stage catalytic conversion of methane under pressure, including steam reforming in the first stage and steam-air reforming in the second stage, using the heat of the gas converted in the second stage, and also additionally
  • a method for producing ammonia which contains the following stages:
  • the presence in the ammonia converter of a large gap between the two shells - the first, providing the catalytic process of ammonia synthesis, and the second (the converter body itself), providing heat transfer through the wall of the first shell from the reaction mixture in the first shell to the flow of the second part of the supplied gas passing through the gap - increases the metal consumption of the body with the diameter of the first shell Di and the size of the gap Z at least by (l + Z/D times, in addition, with a low heat transfer coefficient in the gas-gas system, the relatively small surface of the first shell does not allow for sufficient heat removal of the heat of the ammonia synthesis reaction (92 kJ/mol) released inside the shell for the entire reaction mixture by only the second part of the feedstock flow;
  • a method for producing ammonia and ammonia derivatives from natural gas feedstock includes:
  • the efficiency of the internal combustion engine in terms of fuel consumption - natural gas - is low (efficiency at the level of 50%) and is significantly lower than the efficiency of fire heaters (efficiency at the level of 80-85%);
  • a method for the joint production of ammonia and methanol in a plant comprising a secondary reforming section, a high-temperature carbon monoxide conversion section, a low-temperature carbon monoxide conversion section arranged in a series, a methanol synthesis section and an ammonia synthesis section, characterized in that a gaseous stream containing carbon monoxide, carbon dioxide, hydrogen and water exiting said secondary reforming section is captured, said gaseous stream is fed to a cooling and water separation section, said gaseous stream is cooled a gaseous stream and separating water, feeding a gaseous stream substantially free of water to a methanol synthesis section, feeding a gaseous stream containing carbon monoxide, carbon dioxide, hydrogen and methanol exiting the methanol synthesis section to a methanol separation section, separating a liquid stream containing methanol from a substantially methanol-free gaseous stream containing carbon monoxide, carbon dioxide and hydrogen in said methanol separation section, feeding said substantially methanol
  • the methanol synthesis section (block 23) is designed with multiple reactors arranged in a row to achieve a high degree of reagent conversion, which complicates the process maintenance;
  • a method for the joint production of ammonia and methanol includes reforming of natural gas, utilization of reforming heat, conversion of carbon monoxide, purification of converted gas from carbon dioxide, methanol synthesis, methanation and ammonia synthesis, characterized in that hot converted synthesis gas from primary or secondary reforming is fed into the intertube
  • the post-reforming apparatus which is a shell-and-tube heat exchange reactor, and into the tubes filled with a catalyst - an additional raw steam-gas mixture, which is fed from a common mixing tee or from separate mixing tees, the flow from the inter-tube space for the production of ammonia is fed to the conversion of CO either directly, if the post-reforming is installed after the secondary reforming shaft furnace, or through secondary reforming, if the post-reforming is installed after the primary reforming tubular furnace (patent RU 2663167 C2, IPC C07C 31/04, COIC 1/04, C01B 3/38, declared on 23.08.2016, published on 01.08.2018).
  • the disadvantages of the invention are: the solution to the problem of increasing the productivity of the plant is achieved extensively - by increasing the number of reactors through the use of additional post-reforming and an additional steam generator;
  • a method for producing low-carbon ammonia from natural gas, “Decarbonized Ammonia-3000,” is known, which consists of that on the process line natural gas and steam are heated and subjected to primary reforming, the resulting converted gas is subjected to secondary reforming using a steam-air-oxygen mixture, after which the resulting converted gas is sent to the conversion of carbon dioxide, the resulting synthesis gas is purified from carbon dioxide, then methanation of the purified synthesis gas is carried out, after which ammonia is synthesized, and the purge gas from the ammonia synthesis process is used as fuel for heating natural gas and steam, while on the fuel line natural gas and steam are heated and subjected to primary reforming, the resulting converted gas is subjected to secondary reforming using a steam-air-oxygen mixture, after which the resulting converted gas is sent to the conversion of carbon dioxide, the resulting synthesis gas is purified from carbon dioxide, then the pressure of the purified synthesis gas is reduced and part of it is used as fuel for heating natural gas and steam at fuel
  • the additional fuel line processes natural gas in quantities that are significantly lower than the capacity of the process line, which requires the use of different capacity devices for the same purpose on each of the lines; - the almost doubled number of units operated on two lines sharply increases the risk of emergency situations leading to the shutdown of the entire ammonia production facility.
  • the objective of the claimed invention is to use the material resources of ammonia production to obtain a sought-after product of the third stage of natural gas processing - methanol, to optimize methanol production, to reduce the anthropogenic impact of production on the environment, and to adapt production to harsh natural conditions.
  • the stated problem is solved due to the fact that in the method for producing ammonia and methanol from natural gas based on the method for producing ammonia from natural gas, in which the initial natural gas is successively purified in stages of the process line from sulfur-containing impurities by catalytic hydrotreating and subsequent chemical adsorption of the resulting hydrogen sulfide, heated and subjected to primary reforming, the resulting converted gas is subjected to secondary reforming followed by the conversion of carbon monoxide into carbon dioxide, after which the resulting synthesis gas is purified from carbon dioxide, then methanation of the purified synthesis gas, its adsorption drying and low-temperature rectification are carried out, after which ammonia is synthesized with the formation of high- and low-pressure hydrogen-containing blowdowns, and the heating of the process media - a mixture of the initial natural gas with hydrogen, a mixture of natural gas and water vapor, process air, and superheating of high-pressure steam are carried out by differentially cooling the flue gases of the primary reforming
  • the water treatment unit is supplemented with a source water desalination system in cases where ammonia and methanol production is located in areas with harsh natural conditions that limit the use of fresh water, for example, in gravity-fed marine platforms where only the original seawater is available for performing technological procedures.
  • ammonia also requires nitrogen, while methanol requires carbon oxides. All of these components can be obtained through the conversion of natural hydrocarbon gas, which consists primarily of methane.
  • Natural gas purified from sulfur compounds, is mixed with water vapor, heated by recovering heat from flue gases, and then undergoes a process of steam (primary) reforming.
  • Secondary reforming is a sequential combination of combustion reactions (3) and (4):
  • a third portion of the hydrogen-containing high-pressure blowdown is mixed with hydrogen-containing low-pressure blowdown for use as a carbon-free fuel and/or sent to an integrated methanol synthesis unit, which also utilizes a portion of the carbon dioxide waste.
  • the hydrogen-containing low-pressure blowdown is used as a carbon-free fuel in the primary reformer, thereby replacing natural gas as fuel and reducing carbon dioxide emissions and environmental pollution.
  • Methanol is formed from a mixture of hydrogen and carbon dioxide in a ratio of 3:1 at a temperature of 200-350 °C and a pressure of 5-10 MPa in the presence of three-component copper-containing catalysts via an exothermic reaction (6):
  • the reaction mixture from the reactor is cooled and separated into a liquid phase and a recirculated gas phase, with part of the recirculated gas phase in the form of purge gas and the liquid phase in the form of raw methanol being fed for fractionation to the fractionation section to obtain pure methanol, process water sent to the water treatment unit, and purge gas.
  • the combustion heat of hydrogen-containing low-pressure blowdowns and natural gas in the steam reforming furnace of the ammonia synthesis unit provides both the heating of the process fluids and the subsequent endothermic steam reforming reaction.
  • Heating of all process fluids - the mixture of feedstock natural gas with hydrogen entering the desulfurization, the mixture of natural gas and steam entering the primary reforming, the process air entering the secondary reforming, and the superheated high-pressure steam - is achieved through differential cooling of the flue gases of the primary reforming furnace, which allows for the most complete recovery of heat from the flue gases due to the formation of an optimal sequence of recuperative heat exchangers. Excess heat from secondary reforming is used to generate high-pressure steam.
  • ammonia formed in the ammonia synthesis unit is also useful to use as an additional source of raw material for the synthesis of methanol.
  • low-pressure hydrogen-containing blow-offs which must be compressed to the pressure of high-pressure hydrogen-containing blow-offs and then fed to the methanol synthesis section of the integrated methanol synthesis unit.
  • the integrated methanol synthesis unit prefferably be a methanol production line connected by common flows and a pipeline system with at least two ammonia production lines, which significantly reduces the risk of stopping the production of ammonia and methanol in the event of an emergency in one of the sections or during routine or major repairs.
  • Figure 1 shows a schematic diagram of one of the possible implementation options for the method of producing ammonia and methanol using the following designations: 100 - ammonia production line;
  • the method for producing ammonia and methanol according to the claimed invention is illustrated by a variant of the basic scheme for producing ammonia and methanol, consisting of two identical process lines for producing ammonia 100 and one process line for producing methanol 200, using third parts of the hydrogen-containing high-pressure purges and parts of the carbon dioxide streams from both process lines for producing ammonia 100 in equal quantities.
  • Figure 1 to simplify the description of the operation of producing ammonia and methanol are shown in one process line for obtaining ammonia 100 and in connection with one process line for obtaining methanol 200, since the connection of the process line for obtaining methanol 200 with the second process line for obtaining ammonia 100 is identical.
  • the feedstock natural gas stream from the plant boundaries is sent via pipeline 1 to desulfurization section 102 of the first ammonia production line 100. Since sulfur is a catalytic poison for the catalysts used in the ammonia production process chain, the feedstock natural gas stream is purified from sulfur by means of hydrotreating and chemical adsorption processes in desulfurization section 102. The feedstock natural gas stream is also sent via pipeline 2 to the primary and secondary reforming section 103 for fuel purposes.
  • a stream of purified purge gas from purge gas washing section 112 is sent via pipeline 25 to desulfurization section 102 as a hydrogen source.
  • the hydrotreating process in desulfurization section 102 is carried out in one reactor.
  • the process of chemical binding of sulfur from hydrogen sulfide formed during hydrotreating is carried out in two reactors installed in series. The reactor piping allows for the discharge of spent catalyst without stopping the process.
  • the natural gas stream purified from sulfur compounds, supplied through pipeline 3, is mixed with water vapor supplied through pipeline 10 from the process condensate stripping section 113, heated and then subjected to the primary reforming process in the steam reforming furnace in the primary and secondary reforming section 103.
  • Synthesis gas is produced in furnace tubes filled with a nickel-based catalyst.
  • the heat sources required for the steam reforming process are streams of purified blowdown gas, exhaust regeneration gas, expansion gas, and also raw natural gas supplied to the furnace burners through pipelines 24, 17, 12.
  • the converted gas from the steam reformer and the heated process air enter the secondary reformer reactor where
  • the source of nitrogen for the synthesis of ammonia is a flow of atmospheric air supplied through pipeline 4, which, after filtration and compression on a compressor in the process air compression section 101, is supplied through pipeline 5 to the primary and
  • the converted gas stream is fed via pipeline 6 to the carbon monoxide conversion section 104.
  • Conversion is carried out in two sequentially installed reactors with intermediate heat removal for heating the boiler water.
  • the first reactor uses an iron-based catalyst, while the second uses a copper-based catalyst.
  • the use of two reactors is due to the reduction of the load on the copper catalyst, which is more expensive, but which provides a deeper conversion of CO to CO2.
  • the converted gas stream from the carbon monoxide conversion section 104 is fed via pipeline 7 to the amine gas scrubbing section 105, which removes carbon dioxide from the converted gas stream through absorption with an aqueous amine solution. Carbon dioxide absorption is performed at elevated pressure and reduced temperature. The saturated amine solution is regenerated at reduced pressure and elevated temperature and then reused for absorption (not shown in the figure). Intermediate removal of light gases dissolved in the amine is provided, forming the expansion gas stream, which is sent via pipeline 12 to the primary and secondary reforming section 103 and used as fuel in the steam reforming furnace. The flow of extracted carbon dioxide is removed from the amine gas purification section 105 via pipeline 8, partially sent to the methanol production line 200 via pipeline 43, and the remaining carbon dioxide is sent to the boundaries of the installation via pipeline 37.
  • Oxygen-containing components are contaminants for the ammonia synthesis catalyst, so the final step in syngas purification is methanation—a process in which residual carbon monoxide is converted to methane, which serves as an inert gas during ammonia synthesis.
  • the converted gas stream obtained in amine gas treatment section 105 is sent via pipeline 13 to methanation section 106.
  • the process condensate stream formed during the methanation of synthesis gas in the methanation section 106 is sent through pipeline 14 to the amine gas purification section 105 for mixing with the condensate stream formed during the cooling and separation of the converted gas.
  • the total flow of process condensate is sent through pipeline 9 to the process condensate stripping section 113, where the condensate is purified by stripping with a medium-pressure steam flow supplied through pipeline 29 to the lower part of the stripping column as a stripping agent.
  • the stripping gas stream is fed through pipeline 10 to the primary and secondary reforming section 103 for mixing with the stream of raw natural gas purified from sulfur compounds, fed through pipeline 3.
  • the process condensate stream, purified from impurities of ammonia, methanol and carbon dioxide in the process condensate stripping section 113, is removed from the plant through pipeline 11.
  • the converted gas stream from methanation section 106 enters gas drying section 107 via pipeline 15, where the synthesis gas is purified from water by moisture adsorption on zeolites.
  • the dried gas descends through drying adsorbers and is then filtered to remove entrained zeolite dust.
  • Desiccant regeneration is accomplished at reduced pressure by an ascending flow of regeneration gas supplied via pipeline 18.
  • the heat required for desiccant regeneration is supplied by medium-pressure steam in a regeneration gas heater (not shown).
  • cryogenic gas purification section 108 to remove excess nitrogen, the main amount of methane and part of the argon from the synthesis gas, which are then used as a flow of regeneration gas sent through pipeline 18 to gas drying section 107.
  • cryogenic gas purification section 108 a flow of purified converted gas is generated, fed through pipeline 19 to gas compression section 109, with the nitrogen:hydrogen ratio required for ammonia synthesis, equal to 1:3.
  • the flows of purified converted gas and recycled gas are fed through pipelines 19 and 22, respectively, to gas compression section 109, where the flows are compressed to the pressure required for ammonia synthesis, after which the flow of compressed converted gas is sent through pipeline 20 to ammonia synthesis section 110, where it is heated and sent to a reactor in which ammonia is formed from hydrogen and nitrogen (an exothermic reaction limited by chemical equilibrium).
  • the flow of gas product mixture entering the refrigeration cycle section 111 via pipeline 21 from the ammonia synthesis reactor of the ammonia synthesis section PO is cooled in sequentially installed heat exchangers and then sent to a separator in which the liquid phase, consisting of condensed ammonia, is separated from the gas phase, consisting primarily of unreacted nitrogen and hydrogen, returned in the form of a flow of recirculated gas via pipeline 22 after cold recovery to the gas compression section 109.
  • Refrigeration cycle section 111 consists of an ammonia cooling system, which is an open refrigeration cycle consisting of a refrigerant compressor, a refrigerant condenser, a refrigerant buffer tank, and one or more refrigerant evaporators (not shown in Figure 1).
  • Ammonia is condensed from the gas product mixture stream supplied through pipeline 21 from the ammonia synthesis section 110 in one or more refrigerant evaporators in refrigeration cycle section 111.
  • Refrigerant vapor from the evaporators is directed to the appropriate stages of the refrigerant compressor, which ensures its circulation.
  • the refrigerant from the compressor enters the condenser and then in the liquid phase enters the refrigerant collector (not shown in Figure 1).
  • the flow of liquefied ammonia through pipeline 27 from The refrigeration cycle sections 111 are removed from the plant as a commercial product.
  • the stream of purified purge gas obtained in the purge gas washing section 112 and which is a high-pressure hydrogen-containing purge is partially sent through pipeline 25 to the desulfurization section 102 and is used as a source Hydrogen for hydrotreating the natural gas feedstock is partially fed via pipeline 32 to the methanation section for recycle, and partially sent to the methanol production process needs on the methanol production process line 200 via pipeline 34.
  • the purified blowdown gas stream, obtained in the blowdown gas washing section 112 and representing a low-pressure hydrogen-containing blowdown, is fed via pipeline 24 to the primary and secondary reforming section 103 and used as fuel.
  • the ammonia stream recovered from the blowdown gases is returned via pipeline 26 to the refrigeration cycle section 111.
  • the steam and boiler water system compartment 114 provides deaeration of the demineralized water flow coming from the boundaries of the plant through pipeline 28. Also in the steam system compartment and boiler water 114 provides the supply of prepared boiler water to the process sections for heat recovery and generation of high (in the primary and secondary reforming section 103) and low (in the amine gas cleaning section 105) pressure steam and
  • the second ammonia production line operates similarly to the first, with the same numbering of sections and pipelines. Having two ammonia production lines significantly reduces the risk of ammonia and methanol production shutdowns in the event of an emergency in one section or during routine or major repairs.
  • the methanol production line 200 receives from each of the two ammonia production lines 100
  • the low-pressure carbon dioxide stream enters the carbon dioxide compression section 201 via pipeline 43, where its pressure is increased to a pressure equal in magnitude to the pressure of a third of the high-pressure hydrogen-containing blowdowns, and is fed via pipeline 44 to the methanol synthesis section 202.
  • the carbon dioxide entering the methanol synthesis section 202 under the same pressure via pipeline 44 and the high-pressure hydrogen-containing blowdown via pipeline 34 are mixed, heated, and converted into the target product in the methanol synthesis reactor.
  • the reaction mixture, the methanol synthesis reactor exits cooled, partially condensed and separated into a liquid phase and a recycled gas phase, with part of the recycled gas phase in the form of purge gas and the liquid phase in the form of raw methanol, transported through pipelines 35 and 36, fed to fractionation section 203.
  • high-quality methanol is removed through pipeline 38, purge gas, consisting primarily of ballast nitrogen, through pipeline 39 and process condensate from the methanol synthesis through pipeline 40.
  • Example 2 Using the technology discussed above, a calculation was performed for the combined production of ammonia and methanol in accordance with the claimed invention with a natural gas throughput of 300 t/h.
  • One ammonia production line 100 receives 150 t/h of natural gas.
  • Carbon dioxide and a high-pressure hydrogen-containing purge from both ammonia production lines 100 are fed to methanol production line 200.
  • the calculation results for determining the compositions of the main process streams and their flow rates for one ammonia production line 100 are presented in Table 1.
  • the calculation results for determining the compositions of the main process streams and their flow rates for the common methanol production line 200 are presented in Table 2.
  • the feedstock natural gas contains mercaptans (the concentration of mercaptan sulfur is 0.0063 g/ m3 ), therefore, as a result of hydrotreating, about 1.4 kg/h of mercaptans are converted into hydrogen sulfide, which is then chemisorbed by zinc oxide.
  • the highly purified natural gas stream containing 96.6% methane and about 2.7% Cr-C6 hydrocarbons, is almost completely converted during primary and secondary reforming into synthesis gas, in which The residual methane concentration is 1.32%.
  • the resulting syngas with a carbon monoxide concentration of 8.1%, provides additional hydrogen during carbon monoxide conversion, and the resulting syngas contains approximately 42% hydrogen, 21% nitrogen, and 36% ballast carbon dioxide and water vapor.
  • water vapor is removed from the syngas stream by condensation with the recovery of condensation heat in recuperative heat exchangers.
  • Carbon dioxide is extracted from the syngas stream cooled from 231 to 45°C using an aqueous solution of diethanolamine. Carbon dioxide, which is released as a byproduct of the process during absorbent regeneration, is then used to extract carbon dioxide.
  • Part of the carbon dioxide (5 t/h) is sent to the methanol production line 200, the remaining carbon dioxide can then be used at gas or oil production plants to maintain reservoir pressure, at gas chemical plants for the production of urea, methanol and other products, at food and other industrial plants.
  • the synthesis gas with a hydrogen:nitrogen ratio of 2:1 (the hydrogen concentration is 64.6%, and the nitrogen concentration is 32.3%) is subjected to deep drying and low-temperature rectification, during which excess nitrogen is removed from the synthesis gas and the hydrogen:nitrogen ratio is brought to three to one.
  • carbon dioxide coming from the ammonia production line 100 is compressed from a pressure of 0.14 MPa to 8.52 MPa, mixed with high-pressure hydrogen-containing blowdown, heated, and then synthesized into methanol in a reactor at a temperature of 250-300°C and a pressure of 8.0-8.5 MPa.
  • the resulting reaction mixture is then separated into high-quality commercial methanol, blowdown gas consisting primarily of ballast nitrogen, and methanol synthesis process condensate.
  • a total of 557 tons of marketable product was obtained from the three-stage processing of 300 tons of natural gas per hour.
  • the developed method for producing ammonia and methanol is highly economically efficient. With the cost of feedstock natural gas at $100 per ton, liquid ammonia at $350 per ton, and methanol at $265 per ton, and the company's feedstock costs at $274.4 million per year, revenue from the final product will amount to $1,556 million.
  • the technical result of the claimed method for producing ammonia and methanol from natural gas is the use of material resources from ammonia production to obtain additional in-demand products from the third stage of natural gas processing.
  • methanol gas optimization of methanol production through the efficient separation of high-pressure hydrogen-containing bleeds for fuel use and methanol production, reduction of the anthropogenic impact of production on the environment, adaptation of production to harsh natural conditions, reduction of the risk of cessation of ammonia and methanol production by the enterprise in the event of an emergency in one of the departments or during its routine or major repairs.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention concerne un procédé de production d'ammoniac et de méthanol à partir de gaz naturel, qui consiste purifier le gaz naturel par une adsorption catalytique de purification hydraulique et chimique du sulfure d'hydrogène, le chauffer, le soumettre à un reformage primaire et secondaire suivi de la conversion du monoxyde de carbone en gaz carbonique. Le gaz de synthèse obtenu est purifié pour éliminer le dioxyde de carbone, on effectue une méthanisation, un séchage par adsorption, une rectification à basse température du gaz de synthèse et une synthèse de l'ammoniac afin de générer des flux contenant de l'hydrogène. Le chauffage des milieux industriels se fait grâce aux effluents gazeux du four de reformage primaire, on forme avec les flux contenant de l'hydrogène des flux basse et haute pression, les flux basse pression sont utilisés comme combustible pour le reformage primaire, les flux haute pression sont séparés en parties pour la purification hydraulique catalytique du gaz naturel, le mélange avec le gaz de synthèse avant le séchage et la synthèse de méthanol. L'unité de préparation de l'eau comprend en outre un système de purification de l'eau de départ. Le résultat technique consiste en l'utilisation de ressources matérielles de production d'ammoniac afin de produire du méthanol, une optimisation de la production de méthanol, une diminution de l'impact humain de la production sur le milieu environnant, et une adaptation de la production à des conditions naturelles rudes.
PCT/RU2025/000114 2024-05-29 2025-04-21 Procédé de production d'ammoniac et de méthanol à partir de gaz naturel Pending WO2025250041A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU2024114649 2024-05-29
RU2024114649A RU2832477C1 (ru) 2024-05-29 Способ получения аммиака и метанола из природного газа

Publications (1)

Publication Number Publication Date
WO2025250041A1 true WO2025250041A1 (fr) 2025-12-04

Family

ID=97871230

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/RU2025/000114 Pending WO2025250041A1 (fr) 2024-05-29 2025-04-21 Procédé de production d'ammoniac et de méthanol à partir de gaz naturel

Country Status (1)

Country Link
WO (1) WO2025250041A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU1465410A1 (ru) * 1987-04-30 1989-03-15 Предприятие П/Я Р-6603 Способ получени аммиака и метанола
RU2184702C1 (ru) * 2001-03-21 2002-07-10 Московский государственный университет инженерной экологии Способ получения аммиака
UA48186C2 (uk) * 1995-11-23 2002-08-15 Метанол Казале С.А. Спосіб сумісного виробництва аміаку і метанолу, установка для сумісного виробництва аміаку і метанолу, спосіб модернізації установки синтезу аміаку та спосіб модернізації установки сумісного виробництва аміаку і метанолу
CA2087887C (fr) * 1992-01-23 2003-03-18 Jing Ming Lee Un procede integre servant a produire du methanol et de l'ammoniaque
EA032809B1 (ru) * 2014-12-15 2019-07-31 Хальдор Топсёэ А/С Способ совместного производства аммиака и метанола

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU1465410A1 (ru) * 1987-04-30 1989-03-15 Предприятие П/Я Р-6603 Способ получени аммиака и метанола
CA2087887C (fr) * 1992-01-23 2003-03-18 Jing Ming Lee Un procede integre servant a produire du methanol et de l'ammoniaque
UA48186C2 (uk) * 1995-11-23 2002-08-15 Метанол Казале С.А. Спосіб сумісного виробництва аміаку і метанолу, установка для сумісного виробництва аміаку і метанолу, спосіб модернізації установки синтезу аміаку та спосіб модернізації установки сумісного виробництва аміаку і метанолу
RU2184702C1 (ru) * 2001-03-21 2002-07-10 Московский государственный университет инженерной экологии Способ получения аммиака
EA032809B1 (ru) * 2014-12-15 2019-07-31 Хальдор Топсёэ А/С Способ совместного производства аммиака и метанола

Similar Documents

Publication Publication Date Title
US12054388B2 (en) Systems and methods for production and separation of hydrogen and carbon dioxide
Maxwell Synthetic nitrogen products: a practical guide to the products and processes
US12098658B2 (en) Cogeneration of chemical products
KR102417097B1 (ko) 천연가스를 이용한 블루수소 생산장치와 원료 연소시 발생한 폐가스의 액화 장치, 고온의 증기를 이용한 증기 터빈 발전장치
CN100526273C (zh) 以焦炉气为原料一体化生产液氨和甲醇和/或二甲醚的方法
KR102292411B1 (ko) 수소생산을 위한 석유코크스 합성가스화 공정 중 수성가스전환반응을 통한 고순도 수소생산 시스템
CN102849680A (zh) 从天然气中合成及纯化氢气的方法
NO312026B1 (no) Integrert prosess og integrert anlegg for fremstilling av metanol og ammoniakk
Prasidha et al. Energy-saving and environmentally-benign integrated ammonia production system
US9708543B2 (en) Producing hydrocarbons from catalytic fischer-tropsch reactor
GB2625645A (en) Process for producing hydrogen
US20250242322A1 (en) Method for retrofitting a hydrogen production unit
GB2614780A (en) Method for retrofitting a hydrogen production unit
EA007305B1 (ru) Установка для конверсии замещением и способ управления установкой
CN109153565A (zh) 生产合成气的方法
RU2203214C1 (ru) Способ получения метанола
RU2832477C1 (ru) Способ получения аммиака и метанола из природного газа
RU2832478C1 (ru) Способ получения аммиака из природного газа
US3432265A (en) Ammonia production process
WO2025250042A1 (fr) Procédé de production d'ammoniac à partir de gaz naturel
RU2792583C1 (ru) Способ и установка для синтеза метанола
CN116924331B (zh) 一种天然气制氢系统
CA3218108A1 (fr) Procede et installation de production d'hydrogene pur par reformage a la vapeur avec reduction des emissions de dioxyde de carbone
WO2025253086A1 (fr) Procédé de production d'hydrogène
WO2025253085A1 (fr) Processus de production d'hydrogène

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 25816617

Country of ref document: EP

Kind code of ref document: A1