CN212669206U - Pretreatment system for synthesis ammonia raw material gas - Google Patents

Pretreatment system for synthesis ammonia raw material gas Download PDF

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Publication number
CN212669206U
CN212669206U CN202020962760.1U CN202020962760U CN212669206U CN 212669206 U CN212669206 U CN 212669206U CN 202020962760 U CN202020962760 U CN 202020962760U CN 212669206 U CN212669206 U CN 212669206U
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gas
heat exchanger
plate
low
fin heat
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梁威
刘海军
李忙刚
李腾
董博
王小宁
王连喜
柴自高
张长江
刘浩
谢辉
李�杰
唐小龙
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Xian Shaangu Power Co Ltd
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Xian Shaangu Power Co Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0276—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of H2/N2 mixtures, i.e. of ammonia synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/028—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases
    • F25J3/0285—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases of argon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/20—H2/N2 mixture, i.e. synthesis gas for or purge gas from ammonia synthesis
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/02—Separating impurities in general from the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Abstract

A pretreatment system for synthesis ammonia raw gas comprises a dehydration device, a demercuration device and a cryogenic separation device; the dehydration device is used for cooling and dehydrating the raw material gas; the demercuration device is used for demercuration and purification of dehydration feed gas output by the dehydration device; the cryogenic separation device comprises a plate-fin heat exchanger group and is used for cooling the purified feed gas output by the demercuration device and outputting low-temperature purified feed gas; the cryogenic separation device also comprises a gas-liquid separation unit, wherein the gas-liquid separation unit is used for carrying out gas-liquid separation on the low-temperature purified feed gas output by the plate-fin heat exchanger group to output low-temperature purified gas, and the low-temperature purified gas is heated by the plate-fin heat exchanger group to obtain the feed gas after ammonia synthesis purification. Through the reasonable setting to the part structure, the impurity in the high-efficient desorption ammonia synthesis feed gas to make a CNG product with the impure gas through the mode of rectification purification and export, increased the product added value, adopt the pressure boost inflation of circulation nitrogen gas simultaneously, improve the efficiency, reduce whole device and reform transform cost and operation consumption.

Description

Pretreatment system for synthesis ammonia raw material gas
Technical Field
The utility model belongs to the technical field of the coal chemical industry, concretely relates to synthetic ammonia feed gas pretreatment systems.
Background
The ammonia synthesis reaction in the ammonia synthesis device is a core section of the whole device and an important section for determining the energy consumption of the whole device, the ammonia synthesis reaction has strict requirements on the N/H ratio and the content of the synthetic ammonia raw material gas, and the reaction efficiency of the ammonia synthesis device is reduced and the energy consumption is increased due to impurity gases and inert gases such as methane, argon and the like in the components of the synthetic ammonia raw material gas in the ammonia synthesis.
At present, in the process of updating and eliminating the traditional normal pressure coal gasification mode in China, the main components of the ammonia synthesis feed gas generated by the new alternative coal gasification are as follows: hydrogen (67-72 mol%), nitrogen (22-24 mol%), methane (4-10 mol%), argon (0.4-0.6 mol%), water (saturated state), methane and argon are used as inert gases in the ammonia synthesis section and do not participate in the reaction, a large amount of useless work is consumed in the compression and reaction processes of the system, the energy consumption of the system is increased, the ammonia net value of ammonia synthesis is reduced, and the serious challenge is brought to the ammonia synthesis section of an ammonia synthesis plant. Therefore, the methane and the argon in the synthesis ammonia feed gas are effectively removed, a methane product with economic value is prepared, the additional value of the device is improved, and the method has important practical significance and technical advancement.
Disclosure of Invention
The utility model aims at providing a synthetic ammonia feed gas pretreatment systems, the impurity in the high-efficient desorption ammonia synthesis feed gas to make a CNG product with the impure gas through the mode of rectification purification defeated outward, increased the product added value, adopt the pressure boost expansion of circulating nitrogen gas simultaneously, improve the efficiency, reduce whole device and reform transform the cost and operate the consumption.
In order to solve the technical problem, the utility model discloses a technical scheme is:
a pretreatment system for synthesis ammonia raw gas comprises a dehydration device, a demercuration device and a cryogenic separation device; the dehydration device is used for cooling and dehydrating the raw material gas; the demercuration device is used for demercuration and purification of dehydration feed gas output by the dehydration device; the cryogenic separation device comprises a plate-fin heat exchanger group and is used for cooling the purified feed gas output by the demercuration device and outputting low-temperature purified feed gas; the cryogenic separation device also comprises a gas-liquid separation unit, wherein the gas-liquid separation unit is used for carrying out gas-liquid separation on the low-temperature purified feed gas output by the plate-fin heat exchanger group to output low-temperature purified gas, and the low-temperature purified gas is heated by the plate-fin heat exchanger group to obtain the feed gas after ammonia synthesis purification.
Preferably, the gas-liquid separation unit is also used for carrying out gas-liquid separation on the low-temperature purified feed gas output by the plate-fin heat exchanger group to output liquid methane, and the liquid methane is heated by the plate-fin heat exchanger group to obtain compressed natural gas; the liquid methane is high-purity methane liquid.
Preferably, the gas-liquid separation unit comprises a first dehydrogenation separator, the input end and the output end of the first dehydrogenation separator are connected with the plate-fin heat exchanger set, and the first dehydrogenation separator is used for carrying out gas-liquid two-phase separation on low-temperature purified feed gas output by the plate-fin heat exchanger set and outputting low-temperature purified gas I and first methane low-temperature liquid; heating the low-temperature purified gas I by a plate-fin heat exchanger group to obtain ammonia synthesis purified feed gas I;
the gas-liquid separation unit also comprises a second dehydrogenation separator, the input end and the output end of the second dehydrogenation separator are connected with the plate-fin heat exchanger group, the first methane low-temperature liquid is subjected to pressure reduction gas-liquid two-phase separation through the second dehydrogenation separator after being heated by the plate-fin heat exchanger group, and low-temperature purified gas II and second methane low-temperature liquid are output; and (3) heating the low-temperature purified gas II by using a plate-fin heat exchanger group to obtain the ammonia synthesis purified feed gas II.
Preferably, the gas-liquid separation unit further comprises a methane rectifying tower, the input end of the methane rectifying tower is connected with the output end of the second dehydrogenation separator, and the output end of the methane rectifying tower is connected with the plate-fin heat exchanger group; the methane rectifying tower is used for carrying out gas-liquid two-phase separation on the second methane low-temperature liquid output by the second dehydrogenation separator and outputting liquid methane and non-condensable gas; the liquid methane is heated by the plate-fin heat exchanger group to obtain liquefied natural gas, and the non-condensable gas is heated by the plate-fin heat exchanger group and then is sent out of the cryogenic separation device.
Furthermore, the device also comprises a nitrogen expansion refrigerating device which is used for providing cold energy for the cryogenic separation device through the circulating refrigeration of the circulating nitrogen through compression, cooling and pressurization expansion.
Preferably, the nitrogen expansion refrigeration device comprises a nitrogen compressor and a second cooler which are sequentially connected with the plate-fin heat exchanger group and used for compressing and cooling the nitrogen at normal temperature and low pressure, the output end of the second cooler is connected with the plate-fin heat exchanger group, and the compressed and cooled nitrogen is further cooled by the plate-fin heat exchanger group; the nitrogen expansion refrigeration device also comprises a booster expander, wherein the input end and the output end of the booster expander are connected with the plate-fin heat exchanger group and used for further pressurizing and expanding the high-pressure low-temperature nitrogen output by the plate-fin heat exchanger group for refrigeration and outputting expanded low-temperature nitrogen; one part of the expanded low-temperature nitrogen provides cold energy for the methane rectifying tower, and the other part of the expanded low-temperature nitrogen is heated by the plate-fin heat exchanger group and then is input into the nitrogen compressor for circulation.
Further, the device also comprises a purified gas compression module which is used for compressing the purified gas II of the low-temperature purified gas after the temperature of the plate-fin heat exchanger group is raised and outputting the ammonia synthesis purified feed gas II; the purified gas compression module comprises a purified gas compressor and a third cooler which are sequentially connected, and the low-temperature purified gas II after the temperature of the plate-fin heat exchanger group is compressed and purified by the purified gas compressor and then cooled by the third cooler to obtain the ammonia synthesis purified feed gas II.
Preferably, the demercuration device comprises a demercuration tower and a dust filter which are connected in sequence, and the dehydrated feed gas output by the dehydration device is subjected to demercuration by the demercuration tower and then subjected to dust removal by the dust filter to obtain the purified feed gas.
Preferably, the dehydration device comprises a first cooler, a dehydrator and a drying tower which are connected in sequence, the raw material gas is cooled by the first cooler, and then the dehydrator and the drying tower dehydrate to obtain dehydrated raw material gas.
Preferably, the purified feed gas I and the purified feed gas II after ammonia synthesis are mixed and cooled by a first cooler to obtain purified gas.
Compared with the prior art, the utility model has the advantages that:
(1) the utility model discloses a synthesis ammonia feed gas pretreatment systems, through the reasonable setting to component structure, take the impurity in the method desorption ammonia synthesis feed gas of cryogenic separation and cryogenic rectification, reduce the methane component in the ammonia synthesis feed gas to being less than or equal to 1.2%, guarantee in the ammonia synthesis feed gas that the rate of recovery of hydrogen is greater than or equal to 99.5% when reducing the methane component in the ammonia synthesis feed gas, not only reached the purification requirement and the hydrogen rate of recovery requirement of ammonia synthesis feed gas, and make a CNG product with impurity gas through the mode of rectification purification outward defeated, the product added value has been increased.
(2) The utility model discloses a synthesis ammonia feed gas pretreatment systems, through the reasonable setting to component structure, the refrigeration adopts circulation nitrogen gas pressure boost expansion process, has simplified the flow of ammonia synthesis feed gas cryrogenic separation methane, reduces required cryogen proportioning system investment and area of mixed cryogen compressor by a wide margin, has reduced the device and has reformed transform the cost, is particularly useful for old synthesis ammonia device transformation project.
(3) The utility model discloses a synthesis ammonia feed gas pretreatment systems, through the reasonable setting to the part structure, set up first cooler and dehydrator at dewatering device, through the thick desorption of saturated water cooling with in the feed gas, can improve the adsorption effect of dewatering device drying tower, effectively reduce the regeneration energy consumption basis of drying tower adsorbent by a wide margin, the life cycle of extension device drying tower adsorbent, the whole operation consumption of reduction device.
Drawings
Fig. 1 is a schematic diagram of the connection of the modules of the present invention;
fig. 2 is a schematic diagram of the device connection of the present invention.
The various reference numbers in the drawings have the meanings given below:
1-a dehydration device, 2-a demercuration device, 3-a cryogenic separation device, 4-a nitrogen expansion refrigeration device and 5-a purified gas compression module; 11-a first cooler, 12-a dehydrator and 13-a drying tower; 14-demercuration tower, 15-dust filter; 16-plate-fin heat exchanger group, 17-first dehydrogenation separator, 18-first throttle valve, 19-second dehydrogenation separator, 20-second throttle valve and 21-methane rectifying tower; 22-nitrogen compressor, 23-second cooler, 24-booster expander; 25-purified gas compressor, 26-third cooler.
The following detailed description of the present invention is provided in connection with the accompanying drawings and the detailed description of the invention.
Detailed Description
The following embodiments of the present invention are given, and it should be noted that the present invention is not limited to the following embodiments, and all the equivalent transformations made on the basis of the technical solution of the present application all fall into the protection scope of the present invention.
In the present invention, unless otherwise specified, the use of directional terms such as "upper" and "lower" generally means that the terms are defined with reference to the drawing plane of the corresponding drawing, and "inner" and "outer" mean that the terms are inner and outer relative to the outline of the corresponding part.
The ammonia synthesis raw material gas comprises the following main components: hydrogen (67-72 mol percent), nitrogen (22-24 mol percent), methane (4-10 mol percent), argon (0.4-0.6 mol percent) and water (saturated state), removing impurities in the ammonia synthesis raw material gas by adopting a cryogenic separation and low-temperature rectification method, reducing the methane component in the ammonia synthesis raw material gas to 0.85-1.02 mol percent, and using the pretreated purified gas argon mol percent of 0.33-0.35% as a supplementary assessment index.
The high-purity methane liquid in the utility model is methane liquid with the methane molar content of 92-95%.
A pretreatment system for synthesis ammonia raw gas comprises a dehydration device 1, a demercuration device 2 and a cryogenic separation device 3;
the dehydration device 1 is used for cooling and dehydrating the raw material gas; the function is as follows: cooling the ammonia synthesis feed gas (7.0-8.0 MPa (G) and 40 ℃) from an upstream working section to 10-20 ℃, and removing the water in the feed gas to 1ppmv to carry out the next-stage mercury removal, thereby achieving the purpose of improving the efficiency of the mercury removal process;
the demercuration device 2 is used for demercuration and purification of the dehydration raw material gas output by the dehydration device 1; the function is as follows: the method comprises the steps of leaching sulfur-based activated carbon from dehydrated feed gas to remove trace mercury to 0.01 mu g/Nm3, filtering and purifying dust to 99.9% of particles with the particle size of more than 5 mu m, ensuring that the feed gas H2O entering the next-stage cryogenic separation process is not more than 1ppmv and Hg is not more than 0.01 mu g/Nm3, and achieving the purpose of improving the efficiency of the cryogenic separation process;
the cryogenic separation device 3 comprises a plate-fin heat exchanger group 16, and the plate-fin heat exchanger group 16 is used for cooling the purified feed gas output by the demercuration device 2 and outputting low-temperature purified feed gas; the cryogenic separation device 3 further comprises a gas-liquid separation unit, wherein the gas-liquid separation unit is used for carrying out gas-liquid separation on the low-temperature purified feed gas output by the plate-fin heat exchanger group 16 to output low-temperature purified gas, and the low-temperature purified gas is heated by the plate-fin heat exchanger group 16 to obtain ammonia synthesis purified feed gas;
the function is as follows: the purified feed gas after dehydration and demercuration is cooled to a low-temperature purified feed gas (-160-175 ℃) through the plate-fin heat exchanger group 16, low-temperature purified gas (the mole percentage of methane is 0.85-1.02%, and the mole percentage of argon is 0.33-0.35%) is obtained through gas-liquid separation unit separation, the low-temperature purified gas is subjected to heat exchange with the purified feed gas through the plate-fin heat exchanger group 16, the purified feed gas is output after ammonia synthesis and purification, the methane component in the feed gas after ammonia synthesis and purification is reduced to be less than or equal to 1.2%, and the purification requirement of the ammonia synthesis feed gas is met.
Specifically, the gas-liquid separation unit further performs gas-liquid separation on the low-temperature purified feed gas output by the plate-fin heat exchanger group 16 to output liquid methane, and the liquid methane is heated by the plate-fin heat exchanger group 16 to obtain compressed natural gas; the methane liquid is high-purity methane liquid;
the function is as follows: the low-temperature purification raw material gas (-160 to-175 ℃) output by the plate-fin heat exchanger group 16 is separated by the gas-liquid separation unit to obtain liquid methane, the liquid methane exchanges heat with the purification raw material gas through the plate-fin heat exchanger group 16 and is heated to output compressed natural gas, the purification requirement of the ammonia synthesis raw material gas is met, the recovery rate of hydrogen in the ammonia synthesis raw material gas is ensured to be more than or equal to 99.5%, and the hydrogen recovery rate requirement of the ammonia synthesis raw material gas is met; and the impurity gas is prepared into a CNG product (liquefied natural gas) for outward transportation in a rectification and purification mode, so that the added value of the product is increased.
The gas-liquid separation unit comprises a first dehydrogenation separator 17, the input end and the output end of the first dehydrogenation separator 17 are connected with the plate-fin heat exchanger group 16, and the first dehydrogenation separator 17 is used for carrying out gas-liquid two-phase separation on low-temperature purified feed gas output by the plate-fin heat exchanger group 16 and outputting low-temperature purified gas I and first methane low-temperature liquid; heating the low-temperature purified gas I by a plate-fin heat exchanger group 16 to obtain ammonia synthesis purified feed gas I;
the function is as follows: the first dehydrogenation separator 17 separates gas and liquid phases of the low-temperature purified feed gas to obtain low-temperature purified gas I (-160 to-175 ℃, and the molar percentage of methane is less than or equal to 1%) and first methane low-temperature liquid (-160 to-175 ℃, and the molar percentage of methane is 23 to 38%, the molar percentage of nitrogen is 58 to 71%, and the molar percentage of hydrogen is 4 to 6%), the low-temperature purified gas I exchanges heat with the purified feed gas through the plate-fin heat exchanger group 16, the temperature of the low-temperature purified gas I is raised to obtain ammonia synthesis purified feed gas I (30 to 40 ℃, and the molar percentage of methane is less than or equal to 1%), and the first methane low-temperature;
the gas-liquid separation unit also comprises a second dehydrogenation separator 19, the input end and the output end of the second dehydrogenation separator 19 are connected with the plate-fin heat exchanger group 16, the first methane low-temperature liquid is subjected to pressure reduction gas-liquid two-phase separation through the second dehydrogenation separator 19 after being heated by the plate-fin heat exchanger group 16, and low-temperature purified gas II and second methane low-temperature liquid are output; heating the low-temperature purified gas II by a plate-fin heat exchanger group 16 to obtain ammonia synthesis purified feed gas II;
the function is as follows: the second dehydrogenation separator 19 performs pressure reduction gas-liquid two-phase separation on the first methane low-temperature liquid again, low-temperature purified gas II (3.0-4.0 MPa, -130-150 ℃ and methane mole percent not more than 3.5%) and second methane low-temperature liquid are separated, the low-temperature purified gas II exchanges heat with the purified feed gas through the plate-fin heat exchanger group 16 and is heated to obtain ammonia synthesis purified feed gas II (30-40 ℃ and methane mole percent not more than 3.5%), and the second methane low-temperature liquid is subjected to the next separation process;
wherein, the first methane low-temperature liquid is heated by the plate-fin heat exchanger group 16 and then is transmitted to the second dehydrogenation separator 19 by the first throttle valve 18.
The gas-liquid separation unit also comprises a methane rectifying tower 21, the input end of the methane rectifying tower 21 is connected with the output end of the second dehydrogenation separator 19, and the output end of the methane rectifying tower 21 is connected with the plate-fin heat exchanger group 16; the methane rectifying tower 21 is used for performing gas-liquid two-phase separation on the second methane low-temperature liquid output by the second dehydrogenation separator 19 and outputting liquid methane and non-condensable gas; liquid methane is heated by the plate-fin heat exchanger group 16 to obtain liquefied natural gas, and the non-condensable gas is heated by the plate-fin heat exchanger group 16 and then is sent out of the cryogenic separation device 3;
the function is as follows: separating the second methane low-temperature liquid in a gas-liquid two-phase mode in a methane rectifying tower 21, adjusting the heat quantity at the bottom of the methane rectifying tower 21 and the cold quantity at the top of the methane rectifying tower, wherein the methane-rich liquid has higher methane purity when going downwards, and finally discharging a methane liquid product with the methane content of 92-95% in mole percentage from the bottom of the methane rectifying tower, wherein the methane liquid product is subjected to heat exchange with purified feed gas through a plate-fin heat exchanger group 16 and then is sent out of a cryogenic separation device 3 to be output as a CNG (compressed natural gas) product; the non-condensable gas at the top of the methane rectifying tower 21 exchanges heat with the purified feed gas through the plate-fin heat exchanger group 16, is heated and then is sent out of the cryogenic separation device 3;
wherein, the second methane low-temperature liquid output by the second dehydrogenation separator 19 is transmitted to the methane rectifying tower 21 through the second throttling valve 20.
Specifically, the device also comprises a nitrogen expansion refrigerating device 4, which is used for providing cold energy for the cryogenic separation device 3 through the cyclic refrigeration of compression, cooling and pressurization expansion of the circulating nitrogen;
the nitrogen expansion refrigerating device 4 comprises a nitrogen compressor 22 and a second cooler 23 which are sequentially connected with the plate-fin heat exchanger group 16 and used for compressing and cooling nitrogen at normal temperature and low pressure, the output end of the second cooler 23 is connected with the plate-fin heat exchanger group 16, and the compressed and cooled nitrogen is further cooled through the plate-fin heat exchanger group 16.
The nitrogen expansion refrigerating device 4 further comprises a booster expander 24, wherein the input end and the output end of the booster expander 24 are connected with the plate-fin heat exchanger group 16 and used for further pressurizing and expanding the high-pressure low-temperature nitrogen output by the plate-fin heat exchanger group 16 for refrigeration and outputting expanded low-temperature nitrogen; one part of the expanded low-temperature nitrogen provides cold energy for the methane rectifying tower 21, and the other part of the expanded low-temperature nitrogen is heated by the plate-fin heat exchanger group 16 and then is input into the nitrogen compressor 22 for circulation;
the function is as follows: the circulating nitrogen provides cold for the whole ammonia synthesis raw material gas to remove methane and the CNG product prepared by purifying the methane-rich gas through the circulating refrigeration process of compression, cooling and pressurization expansion, simplifies the process of cryogenic separation of methane from the ammonia synthesis raw material gas, greatly reduces the refrigerant proportioning system investment and the occupied area required by a mixed refrigerant compressor, reduces the device transformation cost, and is very suitable for the old ammonia synthesis device transformation project.
Specifically, the device also comprises a purified gas compression module 5, which is used for compressing the low-temperature purified gas II after the temperature of the plate-fin heat exchanger group 16 is raised and outputting the ammonia synthesis purified feed gas II; the purified gas compression module 5 comprises a purified gas compressor 25 and a third cooler 26 which are connected in sequence, and the low-temperature purified gas II heated by the plate-fin heat exchanger group 16 is compressed and purified by the purified gas compressor 25 and then is cooled by the third cooler 26 to obtain the ammonia synthesis purified feed gas II.
Specifically, the demercuration device 2 comprises a demercuration tower 14 and a dust filter 15 which are connected in sequence, and the dehydrated feed gas output by the dehydration device 1 is demercurated through the demercuration tower 14 and then is dedusted through the dust filter 15 to obtain purified feed gas; the function is as follows: the demercuration tower 14 is used for removing trace mercury in the dehydrated feed gas sulfur-leaching-based active carbon to 0.01 mu g/Nm3The dust filter 15 is used for filtering dust in the feed gas and purifying the dust to more than 5 mu m particles with the removal rate of 99.9 percent, thereby ensuring the feed gas H entering the next-stage cryogenic separation process2O≤1ppmv、Hg≤ 0.01μg/Nm3And the aim of improving the efficiency of the cryogenic separation process is fulfilled.
The dehydration device 1 comprises a first cooler 11, a dehydrator 12 and a drying tower 13 which are connected in sequence, wherein the raw material gas is cooled by the first cooler 11 and dehydrated by the dehydrator 12 and the drying tower 13 to obtain dehydrated raw material gas; the function is as follows: saturated water in the raw material gas is cooled and roughly removed through the first cooler and the dehydrator, so that the adsorption effect of the drying tower of the dehydrating device can be greatly improved, the regeneration energy consumption of the adsorbent of the drying tower is effectively reduced, the service cycle of the adsorbent of the drying tower of the device is prolonged, and the whole operation consumption of the device is reduced.
Specifically, the raw material gas I after ammonia synthesis and purification and the raw material gas II after ammonia synthesis and purification are mixed and cooled by a first cooler 11 to obtain purified gas; the function is as follows: the raw material gas I after ammonia synthesis and purification and the raw material gas II after ammonia synthesis and purification are mixed and cooled by a first cooler 11 to obtain purified gas and are sent to a downstream ammonia synthesis section, wherein the methane component in the purified gas is reduced to the mole percentage of less than or equal to 1.2 percent, and the purification requirement and the hydrogen recovery requirement of the raw material gas for ammonia synthesis are met.
The equipment adopted by each device in the system is the existing equipment.
Examples
The raw material gas of a certain ammonia synthesis working section contains 4 to 10 percent of methane and 0.4 to 0.6 percent of argon by mole percent, the methane in the raw material gas needs to be removed to below 1.5 percent by mole percent and the argon is removed as far as possible according to the requirements of the subsequent ammonia synthesis reaction, and the main volume percent of the raw material gas of the ammonia synthesis working section is as follows:
Figure DEST_PATH_GDA0002859719970000101
the normal-temperature and high-pressure ammonia synthesis raw gas from an upstream working section sequentially enters a first cooler 11, a dehydrator 12 and a drying tower 13 of a dehydration device 1, the raw gas is cooled to 10-20 ℃ and the moisture in the raw gas is removed to 1ppmv, and then trace mercury in the raw gas is removed to 0.01 microgram/Nm in a demercuration tower 14 through sulfur-impregnated activated carbon3. Feed gas entering cryogenic separation device 3 ensures H2O≤1ppmv、Hg≤ 0.01μg/Nm3。
The purified raw material gas after dehydration and demercuration enters a plate-fin heat exchanger group 16, the temperature is reduced to about-160 to-175 ℃, then the purified raw material gas is sent to a first dehydrogenation separator 17 for gas-liquid two-phase separation, low-temperature purified gas I (-160 to-175 ℃ and 0.83 to 0.98 percent of methane mole percentage) and first methane low-temperature liquid are separated, the low-temperature purified gas I is sent to a cryogenic separation device 3 after being subjected to heat exchange and temperature rise with the purified raw material gas through the plate-fin heat exchanger group 16, and is sent to a downstream ammonia synthesis section after being subjected to heat exchange and temperature rise with a first cooler 11.
The first methane low-temperature liquid is heated to-130 to-150 ℃ after part of cold energy is recovered by the plate-fin heat exchanger group 16, and then sent into the second dehydrogenation separator 19 for decompression gas-liquid two-phase separation, low-temperature purified gas II (3.0 to 4.0MPa (G), -140 to-150 ℃ and methane mole percentage 1.9 to 2.5%) and second methane low-temperature liquid are separated, the low-temperature purified gas II is sent out of the cryogenic separation device 3 after being subjected to heat exchange with purified feed gas by the plate-fin heat exchanger group 16 and heated, is compressed by the purified gas compressor 25 and cooled by the third cooler 26 and then is mixed with the purified feed gas I, and the mixed purified gas methane mole percentage is 0.85 to 1.02% and the argon mole percentage is 0.33 to 0.35%.
The second methane low-temperature liquid is throttled further and reduced in pressure to 0.8-1.3 MPa (G), enters the methane rectifying tower 21 from the middle part of the methane rectifying tower 21, the operating temperature of the methane rectifying tower 21 is-130 to-170 ℃, the pressure at the top of the methane rectifying tower is about 0.75MPa (G), finally, a methane liquid product with the methane content of 92-95 mol percent is discharged from the bottom of the methane rectifying tower 21, and the methane liquid product is subjected to heat exchange with the purified feed gas through the plate-fin heat exchanger group 16, is heated and then is sent out of the cryogenic separation device to be output as a CNG (compressed natural gas) product.
The Aspen software is used for carrying out numerical simulation calculation on the thermal data of the device, the hydrogen recovery rate of the synthetic ammonia purge gas reaches 99.5-99.7 mol percent, the impurity gas is removed to 0.85-1.02 mol percent of methane and 0.33-0.35 mol percent of argon, the purge gas completely meets the requirement of ammonia synthesis, and the energy consumption of the subsequent synthetic ammonia can be greatly reduced. The prepared CNG product has the mol percent of methane of 92-95 percent, the mol percent of nitrogen of 2-4 percent and the mol percent of argon of 3-4 percent, and the process power consumption is about 0.45-0.49 kwh/Nm3. The low-temperature cold energy of the purified gas is subjected to heat exchange coupling with the raw material gas of the dehydration device, so that liquid drops in the raw material gas are separated in advance, the dehydration load of the dehydration device can be reduced by about 50-70%, the adsorption effect of a drying tower of the dehydration device can be greatly improved, and the regeneration energy consumption of an adsorbent of the drying tower can be effectively reduced by 200-300 kwh.
The circulating nitrogen pressurization expansion refrigeration process is adopted, the traditional cryogenic methane separation method is simplified, the refrigerant proportioning system investment and the occupied area required by a mixed refrigerant compressor are greatly reduced, the device modification cost is reduced, and the method is very suitable for the old synthetic ammonia device modification project.

Claims (9)

1. A pretreatment system for synthesis ammonia raw gas is characterized by comprising a dehydration device (1), a demercuration device (2) and a cryogenic separation device (3);
the dehydration device (1) is used for cooling and dehydrating the raw material gas;
the demercuration device (2) is used for demercuration and purification of dehydration feed gas output by the dehydration device (1);
the cryogenic separation device (3) comprises a plate-fin heat exchanger group (16), and the plate-fin heat exchanger group (16) is used for cooling the purified feed gas output by the demercuration device (2) and outputting low-temperature purified feed gas;
the cryogenic separation device (3) further comprises a gas-liquid separation unit, the gas-liquid separation unit is used for outputting low-temperature purified gas by gas-liquid separation of the low-temperature purified feed gas output by the plate-fin heat exchanger group (16), and the low-temperature purified gas is heated by the plate-fin heat exchanger group (16) to obtain the feed gas after ammonia synthesis purification.
2. The pretreatment system for synthesis ammonia raw gas according to claim 1, wherein the gas-liquid separation unit further performs gas-liquid separation on the low-temperature purified raw gas output by the plate-fin heat exchanger group (16) to output liquid methane, and the liquid methane is heated by the plate-fin heat exchanger group (16) to obtain compressed natural gas;
the liquid methane is high-purity methane liquid.
3. The pretreatment system for synthesis ammonia raw gas according to claim 2, wherein the gas-liquid separation unit comprises a first dehydrogenation separator (17), the input end and the output end of the first dehydrogenation separator (17) are connected with the plate-fin heat exchanger group (16), and the first dehydrogenation separator (17) is used for carrying out gas-liquid two-phase separation on the low-temperature purified raw gas output by the plate-fin heat exchanger group (16) and outputting a low-temperature purified gas I and a first methane low-temperature liquid; the low-temperature purified gas I is heated by a plate-fin heat exchanger group (16) to obtain ammonia synthesis purified feed gas I;
the gas-liquid separation unit also comprises a second dehydrogenation separator (19), the input end and the output end of the second dehydrogenation separator (19) are connected with the plate-fin heat exchanger group (16), the first methane low-temperature liquid is subjected to pressure reduction gas-liquid two-phase separation through the second dehydrogenation separator (19) after being heated by the plate-fin heat exchanger group (16), and low-temperature purified gas II and second methane low-temperature liquid are output; and the low-temperature purified gas II is heated by a plate-fin heat exchanger group (16) to obtain the ammonia synthesis purified feed gas II.
4. The pretreatment system for a feed gas for ammonia synthesis according to claim 3, wherein the gas-liquid separation unit further comprises a methane rectification column (21), the input end of the methane rectification column (21) is connected with the output end of the second dehydrogenation separator (19), and the output end of the methane rectification column (21) is connected with the plate-fin heat exchanger group (16); the methane rectifying tower (21) is used for carrying out gas-liquid two-phase separation on the second methane low-temperature liquid output by the second dehydrogenation separator (19) and outputting liquid methane and non-condensable gas; the liquefied natural gas is obtained after the liquid methane is heated by the plate-fin heat exchanger group (16), and the non-condensable gas is sent out of the cryogenic separation device (3) after being heated by the plate-fin heat exchanger group (16).
5. A ammonia synthesis feed gas pretreatment system as claimed in claim 4, wherein the plant further comprises a nitrogen expansion refrigeration unit (4) for providing refrigeration to the cryogenic separation unit (3) by cyclic refrigeration of the circulating nitrogen through compression, cooling and pressure-increasing expansion.
6. A pretreatment system for a feed gas for ammonia synthesis according to claim 5, wherein the nitrogen expansion refrigeration device (4) comprises a nitrogen compressor (22) and a second cooler (23) which are connected with the plate-fin heat exchanger group (16) in sequence, and is used for compressing and cooling nitrogen at normal temperature and low pressure, the output end of the second cooler (23) is connected with the plate-fin heat exchanger group (16), and the compressed and cooled nitrogen is further cooled by the plate-fin heat exchanger group (16);
the nitrogen expansion refrigeration device (4) further comprises a booster expander (24), wherein the input end and the output end of the booster expander (24) are connected with the plate-fin heat exchanger group (16) and are used for further pressurizing and expanding the high-pressure low-temperature nitrogen output by the plate-fin heat exchanger group (16) for refrigeration and outputting expanded low-temperature nitrogen;
one part of the expanded low-temperature nitrogen provides cold energy for the methane rectifying tower (21), and the other part of the expanded low-temperature nitrogen is heated by the plate-fin heat exchanger group (16) and then is input into the nitrogen compressor (22) for circulation.
7. The pretreatment system for ammonia synthesis raw gas according to claim 6, wherein the apparatus further comprises a purified gas compression module (5) for compressing the purified gas II purified by the low temperature purified gas heated by the plate-fin heat exchanger group (16) to output the purified raw gas II after ammonia synthesis;
purify gas compression module (5) including the purification gas compressor (25) and third cooler (26) that connect gradually, purify gas II through third cooler (26) cooling after purifying gas compressor (25) compression purification, obtain ammonia synthesis purification back feed gas II by the low temperature purification gas II after plate-fin heat exchanger group (16) heaies up.
8. A pretreatment system for a feed gas for ammonia synthesis according to claim 7, wherein the demercuration apparatus (2) comprises a demercuration tower (14) and a dust filter (15) connected in sequence, and the dehydrated feed gas outputted from the dehydration apparatus (1) is demercurated by the demercuration tower (14) and dedusted by the dust filter (15) to obtain a purified feed gas.
9. A pretreatment system for a raw gas for synthesis ammonia according to claim 8, wherein the dehydration device (1) comprises a first cooler (11), a dehydrator (12) and a drying tower (13) connected in sequence, the raw gas is cooled by the first cooler (11), and then dehydrated by the dehydrator (12) and the drying tower (13) to obtain dehydrated raw gas.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111634883A (en) * 2020-05-29 2020-09-08 西安陕鼓动力股份有限公司 Pretreatment method and system for synthesis ammonia raw material gas

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111634883A (en) * 2020-05-29 2020-09-08 西安陕鼓动力股份有限公司 Pretreatment method and system for synthesis ammonia raw material gas

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