CN117599698A - Method for enlarging production scale of ammonia synthesis device - Google Patents

Method for enlarging production scale of ammonia synthesis device Download PDF

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Publication number
CN117599698A
CN117599698A CN202310949308.XA CN202310949308A CN117599698A CN 117599698 A CN117599698 A CN 117599698A CN 202310949308 A CN202310949308 A CN 202310949308A CN 117599698 A CN117599698 A CN 117599698A
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gas
ammonia
synthesis
synthesis gas
enters
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张洪涛
刘万辉
祝海丽
才力
徐家裕
邵三多
夏铭蒂
高登志
耿乐民
李旭东
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Zhejiang Petroleum and Chemical Co Ltd
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Zhejiang Petroleum and Chemical Co Ltd
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Priority to CN202310949308.XA priority Critical patent/CN117599698A/en
Publication of CN117599698A publication Critical patent/CN117599698A/en
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    • A—HUMAN NECESSITIES
    • A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
    • A01G—HORTICULTURE; CULTIVATION OF VEGETABLES, FLOWERS, RICE, FRUIT, VINES, HOPS OR SEAWEED; FORESTRY; WATERING
    • A01G22/00—Cultivation of specific crops or plants not otherwise provided for
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • 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 in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0417—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
    • 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 in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0458—Separation of NH3
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Botany (AREA)
  • Environmental Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention discloses a method for expanding the production scale of an ammonia synthesis device, which comprises the steps of mixing nitrogen pressurization with hydrogen, carrying out pressure boosting, mixing with outlet gas of a cold exchanger, entering an ammonia cooler, and separating liquid ammonia by an ammonia separator; the gas phase in the ammonia separator passes through a cold exchanger, one part of the gas discharged from the synthesis gas compressor enters a heat exchanger, the other part is introduced from the bottom of the outer cylinder of the reactor, and the annular gap of the inner cylinder and the outer cylinder is discharged after the heat temperature is recovered; the gas discharged from the heat exchanger is divided into two strands and fed into the reactor in parallel, and high-temperature reaction hot gas is collected in a gas collecting pipe at the center of the third bed layer and discharged from the tower; the tower outlet gas directly enters a steam superheater and a furnace water preheater for heat exchange, and enters a heat exchanger tube from the bottom of the heat exchanger; the unreacted synthesis gas enters a water cooler, the unreacted synthesis gas at the outlet of the cold exchanger is mixed with fresh synthesis gas sent out from a synthesis gas compressor, and the mixture enters a primary ammonia separator again to complete a circulating reaction flow of ammonia synthesis; not only can realize energy expansion, but also can reduce the amount of outsourcing liquid ammonia and improve economic benefit.

Description

Method for enlarging production scale of ammonia synthesis device
Technical Field
The invention relates to a production method, in particular to a method for expanding the production scale of an ammonia synthesis device, and belongs to the field of petrochemical industry.
Background
The existing synthetic ammonia production mode is designed to have high methane and argon content (non-condensable gas) in fresh gas, and the discharged air amount of an ammonia synthesis system is large, so that the reduction of carbon emission cannot be realized. Although the fresh gas can be purified through the preamble working section, the content of inert gases such as methane, argon and the like in the fresh gas is controlled below 100ppm, and finally the aim of reducing carbon emission is fulfilled. Meanwhile, the load of the reactor can be increased, but the equipment in the production mode of the synthetic ammonia runs at full load, and the removal of the reaction heat becomes a bottleneck for restricting the load.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a method for expanding the production scale of the ammonia synthesis device, which has the technical characteristics of reducing the amount of outsourcing liquid ammonia, improving economic benefit and the like.
In order to achieve the above purpose, the present invention is realized by the following technical scheme:
a method for scaling up the production of an ammonia plant, the method comprising the steps of:
step 1): the high-purity nitrogen from the air separation device is sent into a nitrogen compressor by a pipe network to be pressurized, mixed with hydrogen from a coal coke gas making device, and then sent into an ammonia synthesis unit as fresh synthesis gas after being pressurized by a pressure increasing section of a synthesis gas compressor; the ammonia synthesis unit comprises a primary ammonia cooler, a secondary ammonia cooler and a secondary ammonia separator;
step 2): mixing fresh synthesis gas with outlet gas of shell side gas phase of a cold exchanger, sequentially entering a primary ammonia cooler and a secondary ammonia cooler, cooling to-12 ℃, entering a secondary ammonia separator, decompressing liquid ammonia separated by the secondary ammonia separator, and delivering;
step 3): the gas phase in the secondary ammonia separator enters a synthesis gas compressor after the temperature is increased to 30 ℃ through a cold exchanger, after the gas is pressurized to 14.1MPa, one part of the gas discharged from the synthesis gas compressor enters a heat exchanger, the other part of the gas is introduced from the bottom of an outer cylinder of a reactor (a synthesis tower), and the gas is discharged from the annular space of the inner cylinder and the outer cylinder after the temperature of the recovered heat is increased to 72 ℃ below zero through the annular space of the inner cylinder and the outer cylinder of the reactor, and enters an inlet of the reactor;
step 4): 50% of the gas discharged from the heat exchanger is divided into two parallel flows into the reactor, and the two flows are converged at the zero-meter screen plate of the catalyst bed (the zero-meter screen plate of the catalyst bed is positioned at the top of the inside of the reactor), sequentially enter three beds in the reactor, undergo synthesis reaction under the action of the catalyst, and release a large amount of heat;
step 5): directly entering the tower gas into a steam superheater, reducing the temperature of the gas to-395 ℃, entering a waste heat boiler (in a pipe), exchanging heat with soft water between pipes of the waste heat boiler, entering the discharged 268 ℃ reaction gas into a furnace water preheater for exchanging heat, reducing the temperature of the reaction gas to-228 ℃, and entering a heat exchanger pipe from the bottom of the heat exchanger to exchange heat with unreacted gas;
step 6): the reaction gas with the temperature reduced to 80 ℃ enters a water cooler, is cooled to 38 ℃, then enters a cold exchange pipe of a cold exchanger to recover cold energy, the temperature is reduced to 22 ℃ below zero, unreacted synthesis gas at the outlet of the cold exchanger is mixed with fresh synthesis gas sent out from a synthesis gas compressor, and enters a primary ammonia separator again to complete the circulation reaction flow of ammonia synthesis;
the water coolers are arranged in two and connected in parallel; the unreacted synthesis gas at the outlet of the water cooler is also directly mixed with fresh synthesis gas fed out of the synthesis gas compressor via a pipeline.
Preferably, 50% of the gas in step 3) is introduced from the bottom of the outer vessel of the reactor (ammonia synthesis column).
Preferably, the high-purity nitrogen (0.4 MPaG) from the air separation device in the step 1) is sent into a nitrogen compressor through a pipe network, is pressurized to 5.25MPaG, is mixed with the hydrogen of 5.0MpaG from the coal coke gas making device, and is then pressurized to 13.3MpaG through a pressure increasing section of a synthetic gas compressor.
Preferably, the synthesis gas compressor comprises a low-pressure cylinder and a high-pressure cylinder which are connected in series, the gas phase in the secondary ammonia separator in the step 3) passes through a cold exchanger, the temperature is increased to 30 ℃ and then enters the high-pressure cylinder in the synthesis gas compressor,
preferably, the unreacted synthesis gas at the outlet of the cold exchanger in step 6) is mixed with fresh synthesis gas from a high pressure cylinder in the synthesis gas compressor.
Preferably, 50% of the gas exiting the heat exchanger is split into two streams and connected to the line feeding the reactor with a start-up furnace.
Preferably, the model of the nitrogen compressor is K0101, the model of the synthesis gas compressor is K0201, the model of the cold exchanger is E0305, the model of the primary ammonia cooler is E0306, the model of the secondary ammonia cooler is E0307, the secondary ammonia separator is V0105, the water cooler is E0304, the heat exchanger is E0303, the steam superheater is E0301, the waste heat boiler is E0302, the model of the boiler water preheater is E0309, the reactor R0301, and the model of the heating furnace is F0301.
The beneficial effects are that: not only can realize energy expansion, but also can reduce the amount of outsourcing liquid ammonia and improve economic benefit.
Drawings
Fig. 1 is a schematic diagram of the overall structure of the present invention.
Detailed Description
The present invention will be further described with reference to the accompanying drawings, but the present invention is not limited to the following examples.
The cost per ton of outsourcing liquid ammonia in actual production is about 1200 yuan/ton higher, the production cost can be greatly reduced by increasing the self yield, and the method for expanding the production scale can expand the load of 18 ten thousand tons per year to 22.5 ten thousand tons per year in the existing synthetic ammonia production, so that the cost can be reduced by about 5400 ten thousand yuan per year.
As shown in fig. 1, a specific embodiment of a method for increasing the production scale of an ammonia plant, which is a method for increasing the production scale of ammonia synthesis, characterized in that the method comprises the steps of:
step 1): the high-purity nitrogen from the air separation device is sent into a nitrogen compressor by a pipe network to be pressurized, mixed with hydrogen from a coal coke gas making device, and then sent into an ammonia synthesis unit as fresh synthesis gas after being pressurized by a pressure increasing section of a synthesis gas compressor; the ammonia synthesis unit comprises a primary ammonia cooler, a secondary ammonia cooler and a secondary ammonia separator;
step 2): mixing fresh synthesis gas with outlet gas of shell side gas phase of a cold exchanger, sequentially entering a primary ammonia cooler and a secondary ammonia cooler, cooling to-12 ℃, entering a secondary ammonia separator, decompressing liquid ammonia separated by the secondary ammonia separator, and delivering;
step 3): the gas phase in the secondary ammonia separator enters a synthesis gas compressor after the temperature is increased to 30 ℃ through a cold exchanger, after the gas is pressurized to 14.1MPa, one part of the gas discharged from the synthesis gas compressor enters a heat exchanger, and the other part of the gas is introduced from the bottom of an outer cylinder of a reactor (ammonia synthesis tower), and after the temperature of heat recovered by an annular gap between an inner cylinder and an outer cylinder of the reactor is increased to 72 ℃, the gas is discharged from the annular gap between the inner cylinder and the outer cylinder and enters an inlet of the reactor;
step 4): 50% of the gas discharged from the heat exchanger is divided into two parallel flows into the reactor, and the two flows are converged at the zero-meter sieve plate of the catalyst bed (the zero-meter sieve plate of the catalyst bed is positioned at the top of the inside of the reactor), and sequentially enter three beds in the reactor, so that synthesis reaction occurs under the action of the catalyst, and a large amount of heat is discharged;
specific: the gas flows along the radial annular space of the upper part from the circumference to the circle center, enters an upper heat insulation section for reaction, enters the shell side of a first bed central heat exchanger in the reactor after the temperature reaches-505 ℃, and enters a second catalyst bed heat insulation section for continuous synthesis reaction after countercurrent heat exchange and temperature reduction with the gas entering the tube side of the first bed central heat exchanger to-390 ℃, enters the shell side of a middle heat exchanger in a second catalyst bed tower after the reaction temperature rises, exchanges heat with the gas entering a second path of auxiliary line of the tower while reacting, cools, then enters a third catalyst bed for reaction, and the gas temperature of the third catalyst bed is-425 ℃, and high-temperature reaction hot gas is collected in a third bed central gas collecting tube and exits the tower;
step 5): directly entering the tower gas into a steam superheater, reducing the temperature of the gas to-395 ℃, entering a waste heat boiler (in a pipe), exchanging heat with soft water between pipes of the waste heat boiler, entering the discharged 268 ℃ reaction gas into a furnace water preheater for exchanging heat, reducing the temperature of the reaction gas to-228 ℃, and entering a heat exchanger pipe from the bottom of the heat exchanger to exchange heat with unreacted gas;
step 6): the reaction gas with the temperature reduced to 80 ℃ enters a water cooler, is cooled to 38 ℃, then enters a cold exchange pipe of a cold exchanger to recover cold energy, the temperature is reduced to 22 ℃ below zero, unreacted synthesis gas at the outlet of the cold exchanger is mixed with fresh synthesis gas sent out from a synthesis gas compressor, and enters a primary ammonia separator again to complete the circulation reaction flow of ammonia synthesis;
the two water coolers are connected in parallel, so that heat removal is increased; the unreacted synthesis gas at the outlet of the water cooler is directly mixed with the fresh synthesis gas sent out from the synthesis gas compressor through a pipeline, so that the temperature regulating auxiliary line of the cold exchanger is increased, part of materials are crossed over the supercooling exchanger, and the heat balance of the cold exchanger is ensured.
The device parameters in the present invention are shown in the following table 1:
the comparison of the present invention with the prior art index is shown in the following Table 2
TABLE 2
Project Before transformation After transformation
Capacity t/d 540 675
Steam production t/tNH 3 0.835 ≥0.85
Boiler water consumption t/tNH 3 0.86 0.875
Consumption t/tNH of circulating water 3 13.5 19.4
KWh/tNH for cold consumption 3 125.5 99.9
Systematic resistance MPa 0.6 0.65
CirculationPower consumption KWh/tNH 3 27.8 22.1
Ammonia net value% 14.7 ≥17
The operation key points of the ammonia synthesis tower are as follows:
1. purpose of gas diversion
The reasonable split flow is an important link for the normal operation of the ammonia synthesis tower (reactor). The gas flow which is split into the upper heat exchanger in the tower is regulated to 50-60%, and the gas flow which is split into the middle heat exchanger is regulated to 50-40%, so that the synthetic reaction temperature curve is more approximate to the optimum temperature curve, the resistance of the synthetic tower is reduced, and the advantages of high yield and energy saving of the synthetic tower are fully exerted.
2. Split flow adjustment operation
1) The gas entering the upper heat exchanger in the tower is unreacted gas heated by the heat exchanger outside the tower, the inlet temperature is 170 ℃ below zero, the gas amount accounts for 50 to 60 percent, and the inlet gas temperature of the middle heat insulation layer and the inlet zero meter gas temperature of the upper heat insulation layer are mainly regulated.
2) The gas entering the middle heat exchanger is unreacted gas heated by the heat exchanger outside the tower, the inlet gas temperature is regulated to 170 ℃ and the gas amount is about 50-40%, and the inlet gas temperature of the lower heat insulation layer and the inlet zero-meter gas temperature of the upper heat insulation layer are mainly regulated.
3) The zero meter temperature can be stabilized between 360 ℃ and 370 ℃, and the hot spot is positioned on the upper heat insulation layer.
4) The temperature of the catalyst in the middle section in the tower is lower than the temperature of the hot spot by 30 ℃, and the temperature of the catalyst in the lower section is lower than the temperature of the hot spot in the middle bed layer by 20 ℃, namely: the upper layer is 490-505 ℃, the middle layer is 460-480 ℃, and the lower layer is 415-435 ℃.
The key point of the invention is that
And (3) controlling the system flow: the fresh gas is lifted to 13.55MPaG by a pressurizing circulating machine, mixed with the outlet gas of a cold exchanger, sequentially enters a primary ammonia cooler and a secondary ammonia cooler, cooled to-12 ℃, enters a secondary ammonia separator and a cold exchanger, and enters a circulating section of the pressurizing circulating machine after the temperature is raised to 30 ℃, and the gas is pressurized to 14.1MPa.
About 50% of the gas discharged from the synthesis gas compressor is introduced from the bottom of the outer cylinder of the synthesis tower, and the gas is discharged from the annular space after the temperature of the heat recovered by the annular space of the inner cylinder and the outer cylinder is raised to 72 ℃; in addition, about 50% of the gas is heated to 170 ℃ by an external heat exchanger of the tower, two gas flows are connected in parallel into the tower, the two gas flows are converged at a zero-meter screen plate of the catalyst bed and pass through an annular space of an upper radial basket together, the gas flows from the circumference to the circle center direction radially, enters an upper heat insulation section for reaction, enters a shell pass of a first bed central heat exchanger after the temperature reaches 505 ℃, and enters a second catalyst bed heat insulation section for continuous synthetic reaction after countercurrent heat exchange and cooling with the gas entering the tube pass of the heat exchanger, enters the shell pass of a middle heat exchanger in the second catalyst bed tower after the temperature of the reaction is raised, and enters a third catalyst bed for reaction while heat exchange and cooling with the gas entering a second path of auxiliary line of the tower, and the gas temperature of the third catalyst bed is 425 ℃, the high-temperature reaction hot gas is collected in a gas collecting pipe outlet tower at the center of a third bed layer, the outlet tower gas directly enters a steam superheater, the gas temperature is reduced to be about 395 ℃ and enters a waste heat boiler pipe, the reaction gas which is discharged after heat exchange with soft water between pipes enters a soft water heater heating boiler for supplying water, the reaction gas is reduced to be about 228 ℃ and enters a heat exchanger pipe outside the tower, heat exchange is carried out between the reaction gas and unreacted gas, the reaction gas with the temperature reduced to be about 80 ℃ enters a water cooler, the reaction gas is cooled to be about 38 ℃, then enters a cold exchange pipe for recovering cold energy, the temperature is reduced to be about 22 ℃ and then enters a two-stage ammonia cooler sequentially after being combined with fresh gas at an outlet of a synthetic gas compressor, the temperature is reduced to be-12 ℃ after part of liquid ammonia is separated, and the separated liquid ammonia enters an ammonia separator and is discharged out of the device; the gas phase enters a cold exchange tube, the temperature is increased to about 30 ℃ after the cold energy is recovered, and the gas phase enters a circulation section of a synthetic gas circulation machine for pressure increasing to carry out a new cycle.
In a preferred embodiment, 50% of the gas in step 3) is introduced from the bottom of the outer vessel of the reactor (ammonia synthesis column).
In the preferred embodiment, in the step 1), high-purity nitrogen (0.4 MPaG) from the air separation device is sent into a nitrogen compressor through a pipe network, is pressurized to 5.25MPaG, is mixed with 5.0MpaG of hydrogen from a coal tar gas making device, and is then pressurized to 13.3MpaG through a pressure increasing section of a synthetic gas compressor.
In a preferred embodiment, the synthesis gas compressor comprises a low pressure cylinder and a high pressure cylinder connected in series, and the gas phase in the secondary ammonia separator in step 3) passes through a cold exchanger and enters the high pressure cylinder in the synthesis gas compressor after the temperature is increased to 30 ℃.
In a preferred embodiment, the unreacted synthesis gas at the outlet of the cold exchanger in step 6) is mixed with fresh synthesis gas from a high pressure cylinder in the synthesis gas compressor.
In a preferred embodiment, 50% of the gas exiting the heat exchanger is split into two streams and fed into the reactor in a pipeline connected to a start-up furnace.
In a preferred embodiment mode, the model of the nitrogen compressor is K0101, the model of the synthesis gas compressor is K0201, the model of the cold exchanger is E0305, the model of the primary ammonia cooler is E0306, the model of the secondary ammonia cooler is E0307, the model of the secondary ammonia separator is V0105, the water cooler is E0304, the heat exchanger is E0303, the steam superheater is E0301, the waste heat boiler is E0302, the model of the boiler water preheater is E0309, the reactor is R0301 (ammonia synthesis tower), and the model of the heating furnace for starting is F0301.
Finally, it should be noted that the invention is not limited to the above embodiments, but that many variants are possible. All modifications directly derived or suggested to one skilled in the art from the present disclosure should be considered as being within the scope of the present invention.

Claims (7)

1. A method for scaling up the production of an ammonia plant, the method comprising the steps of:
step 1): the high-purity nitrogen from the air separation device is sent into a nitrogen compressor by a pipe network to be pressurized, mixed with hydrogen from a coal coke gas making device, and then sent into an ammonia synthesis unit as fresh synthesis gas after being pressurized by a pressure increasing section of a synthesis gas compressor; the ammonia synthesis unit comprises a primary ammonia cooler, a secondary ammonia cooler and a secondary ammonia separator;
step 2): mixing fresh synthesis gas with outlet gas of shell side gas phase of a cold exchanger, sequentially entering a primary ammonia cooler and a secondary ammonia cooler, cooling to-12 ℃, entering a secondary ammonia separator, decompressing liquid ammonia separated by the secondary ammonia separator, and delivering;
step 3): the gas phase in the secondary ammonia separator passes through a cold exchanger, the temperature is increased to 30 ℃ and then enters a synthesis gas compressor, after the gas is pressurized to 14.1MPa, part of the gas discharged from the synthesis gas compressor enters a heat exchanger, the other part of the gas discharged from the synthesis gas compressor is introduced from the bottom of an outer cylinder of the reactor, and the heat is recovered through the annular gap between the inner cylinder and the outer cylinder of the reactor, and after the temperature is increased to 72 ℃, the annular gap between the inner cylinder and the outer cylinder is discharged and enters an inlet of the reactor;
step 4): 50% of the gas discharged from the heat exchanger is divided into two paths which are connected in parallel and enter the reactor, the two paths of gas are converged at the zero-meter screen plate of the catalyst bed, and sequentially enter three beds in the reactor, and the gas is subjected to synthesis reaction under the action of the catalyst and emits a large amount of heat;
step 5): directly entering the tower gas into a steam superheater, reducing the temperature of the gas to-395 ℃, entering a waste heat boiler (in a pipe), exchanging heat with soft water between pipes of the waste heat boiler, entering the discharged 268 ℃ reaction gas into a furnace water preheater for exchanging heat, reducing the temperature of the reaction gas to-228 ℃, and entering a heat exchanger pipe from the bottom of the heat exchanger to exchange heat with unreacted gas;
step 6): the reaction gas with the temperature reduced to 80 ℃ enters a water cooler, is cooled to 38 ℃, then enters a cold exchange pipe of a cold exchanger to recover cold energy, the temperature is reduced to 22 ℃ below zero, unreacted synthesis gas at the outlet of the cold exchanger is mixed with fresh synthesis gas sent out from a synthesis gas compressor, and enters a primary ammonia separator again to complete the circulation reaction flow of ammonia synthesis;
the water coolers are arranged in two and connected in parallel; the unreacted synthesis gas at the outlet of the water cooler is also directly mixed with fresh synthesis gas fed out of the synthesis gas compressor via a pipeline.
2. A method for scaling up the production of an ammonia plant according to claim 1, wherein: in step 3), 50% of the gas was introduced from the bottom of the outer tub of the reactor (synthesis column).
3. A method for scaling up the production of an ammonia plant according to claim 1, wherein: and in the step 1), 0.4MPaG of high-purity nitrogen from the air separation device is sent into a nitrogen compressor through a pipe network, is pressurized to 5.25MPaG, is mixed with 5.0MpaG of hydrogen from a coal coke gas making device, and is then pressurized to 13.3MpaG through a pressure increasing section of a synthetic gas compressor.
4. A method for scaling up the production of an ammonia plant according to claim 1, wherein: the synthesis gas compressor comprises a low-pressure cylinder and a high-pressure cylinder which are connected in series, and the gas phase in the secondary ammonia separator in the step 3) passes through a cold exchanger, and enters the high-pressure cylinder in the synthesis gas compressor after the temperature is increased to 30 ℃.
5. A method for scaling up a production of an ammonia plant according to claim 4, wherein: and 6) mixing the unreacted synthesis gas at the outlet of the intercooled exchanger with fresh synthesis gas sent out by a high-pressure cylinder in a synthesis gas compressor.
6. A method for scaling up a production of an ammonia plant according to claim 4, wherein: 50% of the gas exiting the heat exchanger is divided into two paths and connected with a start-up heating furnace on a pipeline which is connected into the reactor in parallel.
7. A method for scaling up a production of an ammonia plant according to claim 4, wherein: the model of the nitrogen compressor is K0101, the model of the synthesis gas compressor is K0201, the model of the cold exchanger is E0305, the model of the primary ammonia cooler is E0306, the model of the secondary ammonia cooler is E0307, the secondary ammonia separator is V0105, the water cooler is E0304, the heat exchanger is E0303, the steam superheater is E0301, the waste heat boiler is E0302, the model of the boiler water preheater is E0309, the reactor R0301, and the model of the starting heating furnace is F0301.
CN202310949308.XA 2023-07-31 2023-07-31 Method for enlarging production scale of ammonia synthesis device Pending CN117599698A (en)

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