CN110127611A - Ammonia synthesis process raw material gas shift heating system - Google Patents
Ammonia synthesis process raw material gas shift heating system Download PDFInfo
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- CN110127611A CN110127611A CN201910410951.9A CN201910410951A CN110127611A CN 110127611 A CN110127611 A CN 110127611A CN 201910410951 A CN201910410951 A CN 201910410951A CN 110127611 A CN110127611 A CN 110127611A
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- gas
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- exchange pipeline
- feed
- raw material
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 64
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000002994 raw material Substances 0.000 title claims abstract description 29
- 238000010438 heat treatment Methods 0.000 title claims abstract description 28
- 230000008569 process Effects 0.000 title claims abstract description 28
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 26
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 25
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 17
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 14
- 238000002407 reforming Methods 0.000 claims abstract description 14
- 230000003647 oxidation Effects 0.000 claims abstract description 7
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 7
- 230000002194 synthesizing effect Effects 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 149
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 230000008929 regeneration Effects 0.000 claims description 21
- 238000011069 regeneration method Methods 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 230000008859 change Effects 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 5
- 238000006392 deoxygenation reaction Methods 0.000 claims description 3
- 238000003303 reheating Methods 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 238000001816 cooling Methods 0.000 claims description 2
- 239000012141 concentrate Substances 0.000 abstract description 9
- 238000005265 energy consumption Methods 0.000 abstract description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000000567 combustion gas Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
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
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- 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
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/047—Composition of the impurity the impurity being carbon monoxide
-
- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention belongs to ammonia synthesizing industry technical fields.Ammonia synthesis process raw material gas shift heating system includes the first feed gas heater, raw material feed channel, concentrates preheating furnace, primary reformer, secondary reformer, reforming gas boiler, the preheating of the second unstripped gas, the heat that secondary reformer methane, Oxidation of Carbon Monoxide generate is made full use of by primary reformer, reforming gas boiler, the first feed gas heater, the second feed gas heater, has saved energy consumption.Preheating furnace is concentrated to be equipped with the first heat exchange pipeline, the second heat exchange pipeline, third heat exchange pipeline, the 4th heat exchange pipeline simultaneously, using the temperature difference for concentrating preheating furnace different location, reasonable arrangement heat exchange improves the utilization rate of thermal energy.
Description
Technical field
The present invention relates to ammonia synthesizing industry technical field more particularly to a kind of ammonia synthesis process raw material gas shift heat supply systems
System.
Background technique
Industry synthetic ammonia is that hydrogen and nitrogen react generation under the action of certain temperature, pressure and catalyst.Raw material
In hydrogen by natural gas, oven gas etc. pass through a series of chemical reaction generate.First specially in natural gas or oven gas
Alkane and water react under the action of certain temperature, pressure and catalyst generates hydrogen and carbon monoxide.Since carbon monoxide can
Lead to the catalyst poisoning during ammonia synthesis reaction, it is therefore desirable in certain temperature, pressure and be urged with water and carbon monoxide
Reaction generates hydrogen and carbon dioxide under the action of agent, to remove carbon monoxide, then uses solution absorbing carbon dioxide again,
So that the hydrogen of preparation becomes pure.Because this series of chemical reaction requires a large amount of heat, many heating are needed
Furnace come for reaction heat is provided.The heat loss of heating furnace is mainly flue gas loss and heat loss due to incomplete combustion.Therefore stove
Quantity is more, and flue gas loss is bigger.
Summary of the invention
In view of this, it is necessary to provide the ammonia synthesis process unstripped gas of a kind of reduction heating furnace quantity, raising heat utilization efficiency
Convert heating system.
Ammonia synthesis process raw material gas shift heating system includes the first feed gas heater, raw material feed channel, concentrates preheating
Furnace, primary reformer, secondary reformer, reforming gas boiler, the second feed gas heater, first feed gas heater are interior equipped with low
The air inlet of the low-temperature heat exchange pipeline of warm heat exchange pipeline and high-temperature heat exchange tube road, the raw material feed channel and the first feed gas heater
Mouth is connected to, and is successively arranged the first heat exchange pipeline, the second heat exchange pipeline, third heat exchanger tube from top to bottom in the concentration preheating furnace
Road, the 4th heat exchange pipeline, the gas outlet of the low-temperature heat exchange pipeline of the first feed gas heater and the first heat exchange for concentrating preheating furnace
The air inlet of pipeline is connected to, and the gas outlet of the first heat exchange pipeline is connected to the feed inlet of primary reformer, the unstripped gas after heating
It is passed through in primary reformer and is reacted, the discharge port of primary reformer is connected to the feed inlet of secondary reformer, by the raw material after reacting
Gas, which is passed through secondary reformer and reacts with oxygen, is made conversion gas, the discharge port of secondary reformer and the heat exchanger tube of reforming gas boiler
Road connection, to be heated using the heat in conversion gas to the material in reforming gas boiler, reforming gas boiler
The gas outlet of heat exchange pipeline is connected to the high-temperature heat exchange tube road of the first feed gas heater, with the raw material in low-temperature heat exchange pipeline
Gas exchanges heat, and the gas outlet in the high-temperature heat exchange tube road of the first feed gas heater and the high temperature of the second feed gas heater exchange heat
The air inlet of pipeline is connected to, the middle change furnace in the gas outlet and ammonia synthesis process in the high-temperature heat exchange tube road of the second feed gas heater
Feed inlet connection, by cooling after conversion gas be introduced into become furnace；The low-temperature heat exchange pipeline of second feed gas heater
Air inlet be connected to the gas outlet of the 4th heat exchange pipeline of preheating furnace is concentrated, the air inlet of the 4th heat exchange pipeline with synthesize ammonia work
The raw material feed channel of skill is connected to, to heat unstripped gas by the 4th heat exchange pipeline and the second feed gas heater；The third is changed
The inlet of heat pipeline is connected to the deoxygenation waterpipe of ammonia synthesis process, the liquid outlet of third heat exchange pipeline and ammonia synthesis process
Middle change furnace is connected to, and becomes furnace and and reaction of carbon monoxide in the deaerated water importing after heating；Second heat exchange pipeline into
Port is connected to oxygen-enriched pipeline, and the gas outlet of the second heat exchange pipeline is connected to the feed inlet of secondary reformer so that in unstripped gas not by
The methane and Oxidation of Carbon Monoxide of conversion.
Preferably, the liquid outlet of second heat exchange pipeline is also connected to the water inlet for synthesizing useless pot, with to deaerated water into
Row reheating.
Preferably, the ammonia synthesis process raw material gas shift heating system further includes regeneration gas surge tank, the regeneration gas
The air inlet of surge tank is connected to the air inlet of regeneration feed channel, the gas outlet of regeneration gas surge tank and the combustion gas for concentrating preheating furnace
Nozzle connection, to provide fuel to concentration preheating furnace.
The utility model has the advantages that ammonia synthesis process raw material gas shift heating system of the invention includes the first feed gas heater, original
Expect feed channel, concentrate preheating furnace, primary reformer, secondary reformer, reforming gas boiler, the preheating of the second unstripped gas, secondary reformer methane, one
The heat of oxidation of coal generation is aoxidized by primary reformer, reforming gas boiler, the first feed gas heater, the second feed gas heater
It makes full use of, has saved energy consumption.Simultaneously concentrate preheating furnace be equipped with the first heat exchange pipeline, the second heat exchange pipeline, third heat exchange pipeline,
4th heat exchange pipeline, using the temperature difference for concentrating preheating furnace different location, reasonable arrangement heat exchange improves the utilization of thermal energy
Rate.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of ammonia synthesis process raw material gas shift heating system of the invention.
In figure: the first feed gas heater 10, concentrates preheating furnace 30, the first heat exchange pipeline 301, the at raw material feed channel 20
Two heat exchange pipelines 302, third heat exchange pipeline 303, the 4th heat exchange pipeline 304, primary reformer 40, secondary reformer 50, conversion gas waste heat boiler
Furnace 60, the second feed gas heater 70 synthesize useless pot 80, regeneration gas surge tank 90, middle change furnace 100.
Specific embodiment
In order to illustrate the technical solution of the embodiments of the present invention more clearly, below will be to needed in the embodiment attached
Figure is briefly described, it should be apparent that, drawings in the following description are some embodiments of the invention, common for this field
For technical staff, without creative efforts, it is also possible to obtain other drawings based on these drawings.
Fig. 1 is please referred to, ammonia synthesis process raw material gas shift heating system includes the first feed gas heater 10, raw material tracheae
Preheating furnace 30, primary reformer 40, secondary reformer 50, reforming gas boiler 60, the second feed gas heater 70 are concentrated in road 20, described
Low-temperature heat exchange pipeline and high-temperature heat exchange tube road, the raw material feed channel 20 and the first raw material are equipped in first feed gas heater 10
The air inlet of the low-temperature heat exchange pipeline of air preheater 10 is connected to, and is successively arranged first from top to bottom in the concentration preheating furnace 30 and is changed
Heat pipeline 301, the second heat exchange pipeline 302, third heat exchange pipeline 303, the 4th heat exchange pipeline 304, the first feed gas heater 10
The gas outlet of low-temperature heat exchange pipeline be connected to the air inlet of the first heat exchange pipeline 301 of preheating furnace 30 is concentrated, the first heat exchanger tube
The gas outlet in road 301 is connected to the feed inlet of primary reformer 40, and the unstripped gas after heating is passed through in primary reformer 40 and is reacted,
The discharge port of primary reformer 40 is connected to the feed inlet of secondary reformer 50, by the unstripped gas after reacting be passed through secondary reformer 50 and with
Oxygen, which reacts, is made conversion gas, and the discharge port of secondary reformer 50 is connected to the heat exchange pipeline of reforming gas boiler 60, with benefit
The material in reforming gas boiler 60 is heated with the heat in conversion gas, the heat exchange pipeline of reforming gas boiler 60
Gas outlet be connected to the high-temperature heat exchange tube road of the first feed gas heater 10, with in low-temperature heat exchange pipeline unstripped gas carry out
Heat exchange, the high-temperature heat exchange tube of the gas outlet in the high-temperature heat exchange tube road of the first feed gas heater 10 and the second feed gas heater 70
The air inlet in road is connected to, the middle change furnace in the gas outlet and ammonia synthesis process in the high-temperature heat exchange tube road of the second feed gas heater 70
100 feed inlet connection, the conversion gas after cool down be introduced into change furnace 100；The low temperature of second feed gas heater 70
The air inlet of heat exchange pipeline is connected to the gas outlet for the 4th heat exchange pipeline 304 for concentrating preheating furnace 30, the 4th heat exchange pipeline 304
Air inlet is connected to the raw material feed channel 20 of ammonia synthesis process, to pass through the 4th heat exchange pipeline 304 and the second feed gas heater
70 heating unstripped gas；The inlet of the third heat exchange pipeline 303 is connected to the deoxygenation waterpipe of ammonia synthesis process, third heat exchange
The liquid outlet of pipeline 303 is connected to the middle change furnace 100 of ammonia synthesis process, becomes furnace 100 simultaneously in the deaerated water importing after heating
With reaction of carbon monoxide；The air inlet of second heat exchange pipeline 302 is connected to oxygen-enriched pipeline, and the second heat exchange pipeline 302 goes out
Port is connected to the feed inlet of secondary reformer 50, so that the methane and Oxidation of Carbon Monoxide that are not converted in unstripped gas.
First feed gas heater 10 and the second feed gas heater 70 all contain high-temperature heat exchange tube road and low-temperature heat exchange pipe
Road.High-temperature heat exchange tube road and low-temperature heat exchange pipeline are arranged parallel to exchange heat.
Further, the liquid outlet of second heat exchange pipeline 302 is also connected to the water inlet for synthesizing useless pot 80, with to removing
Oxygen water carries out reheating.
Further, the ammonia synthesis process raw material gas shift heating system further includes regeneration gas surge tank 90, it is described again
The air inlet of angry surge tank 90 is connected to the air inlet of regeneration feed channel, and the gas outlet of regeneration gas surge tank 90 and concentration preheat
The gas nozzle of furnace 30 is connected to, to provide fuel to concentration preheating furnace 30.
Concentrate the regeneration gas in preheating furnace 30 behind three sections of feed gas compressor outlets and unstripped gas temp.-changing adsorption
Regeneration, many impurity are contained in the inside.Regeneration gas surge tank 90 can be such that these impurity fall by standing, to improve combustion gas
Clean level.Simultaneously because the generation of regeneration gas is unstable, regeneration gas surge tank 90 can play the function of storage combustion gas.When
When regeneration gas is more, just it is stored in regeneration gas surge tank 90；If regeneration gas supply tails off, concentrate in preheating furnace 30
Combustion gas can be supplemented by the combustion gas in regeneration gas surge tank 90.
It concentrates and is equipped with the first heat exchange pipeline 301, the second heat exchange pipeline 302, third heat exchange pipeline 303, the in preheating furnace 30
Four heat exchange pipelines 304, the first heat exchange pipeline 301 contain steam feed gas for heating, i.e., heating methane etc. is for synthesizing ammonia
Unstrpped gas；Second heat exchange pipeline 302 is for heating oxygen-enriched air, and the oxygen-enriched air being heated is for remaining in secondary reformer 50
The oxidation of methane and carbon monoxide；Third heat exchange pipeline 303 for heating deaerated water, deaerated water be used in middle changes furnace 100 and
Reaction of carbon monoxide prepares hydrogen；4th heat exchange pipeline 304 is used to heat the unstripped gas without containing steam, subsequent not contain steam
Unstripped gas also heated by the second feed gas heater 70, to improve the temperature of unstripped gas.It is sent out in subsequent unstripped gas and steam
When raw reaction, since with certain initial temperature, the energy consumption for reaching predetermined temperature will be reduced.It is pre- for the second unstripped gas
The thermal energy that hot device 70 provides the methane of thermal energy come from secondary reformer 50 in unstripped gas and Oxidation of Carbon Monoxide is discharged, benefit
Heat exchange is carried out with the heat in unstripped gas to be also beneficial to reduce energy consumption.Whole flow process, which takes full advantage of, concentrates preheating furnace 30 and original
Thermal energy after expecting solid/liquid/gas reactions, reduces the use of heating furnace, largely eliminates flue gas loss.
The above disclosure is only the preferred embodiments of the present invention, cannot limit the right model of the present invention with this certainly
It encloses, those skilled in the art can understand all or part of the processes for realizing the above embodiment, and wants according to right of the present invention
Made equivalent variations is sought, is still belonged to the scope covered by the invention.
Claims (3)
1. ammonia synthesis process raw material gas shift heating system, it is characterised in that: including the first feed gas heater, raw material tracheae
Preheating furnace, primary reformer, secondary reformer, reforming gas boiler, the second feed gas heater are concentrated in road, and first unstripped gas is pre-
Low-temperature heat exchange pipeline and high-temperature heat exchange tube road are equipped in hot device, the low temperature of the raw material feed channel and the first feed gas heater changes
The air inlet of heat pipeline is connected to, be successively arranged from top to bottom in the concentration preheating furnace the first heat exchange pipeline, the second heat exchange pipeline,
Third heat exchange pipeline, the 4th heat exchange pipeline, the gas outlet of the low-temperature heat exchange pipeline of the first feed gas heater and concentration preheating furnace
The first heat exchange pipeline air inlet connection, the gas outlet of the first heat exchange pipeline is connected to the feed inlet of primary reformer, will heat
Unstripped gas afterwards, which is passed through in primary reformer, to be reacted, and the discharge port of primary reformer is connected to the feed inlet of secondary reformer, will be occurred anti-
Unstripped gas after answering, which is passed through secondary reformer and reacts with oxygen, is made conversion gas, the discharge port and conversion gas waste heat boiler of secondary reformer
The heat exchange pipeline of furnace is connected to, and to heat using the heat in conversion gas to the material in reforming gas boiler, converts gas
The gas outlet of the heat exchange pipeline of waste heat boiler is connected to the high-temperature heat exchange tube road of the first feed gas heater, with low-temperature heat exchange pipe
Unstripped gas in road exchanges heat, the gas outlet in the high-temperature heat exchange tube road of the first feed gas heater and the second feed gas heater
High-temperature heat exchange tube road air inlet connection, the gas outlet in the high-temperature heat exchange tube road of the second feed gas heater and ammonia synthesis process
In middle change furnace feed inlet connection, by cooling after conversion gas be introduced into become furnace；Second feed gas heater it is low
The air inlet of warm heat exchange pipeline is connected to the gas outlet for the 4th heat exchange pipeline for concentrating preheating furnace, the air inlet of the 4th heat exchange pipeline
It is connected to the raw material feed channel of ammonia synthesis process, to heat unstripped gas by the 4th heat exchange pipeline and the second feed gas heater；
The inlet of the third heat exchange pipeline is connected to the deoxygenation waterpipe of ammonia synthesis process, the liquid outlet of third heat exchange pipeline and conjunction
It is connected at the middle change furnace of ammonia process, becomes furnace and and reaction of carbon monoxide in the deaerated water importing after heating；Described second changes
The air inlet of heat pipeline is connected to oxygen-enriched pipeline, and the gas outlet of the second heat exchange pipeline is connected to the feed inlet of secondary reformer, so that former
The methane and Oxidation of Carbon Monoxide not being converted in material gas.
2. ammonia synthesis process raw material gas shift heating system as described in claim 1, it is characterised in that: second heat exchanger tube
The liquid outlet in road is also connected to the water inlet for synthesizing useless pot, to carry out reheating to deaerated water.
3. ammonia synthesis process raw material gas shift heating system as described in claim 1, it is characterised in that: the ammonia synthesis process
Raw material gas shift heating system further includes regeneration gas surge tank, the air inlet of the regeneration gas surge tank and regeneration feed channel into
Port connection, the gas outlet of regeneration gas surge tank are connected to the gas nozzle of preheating furnace is concentrated, to provide combustion to concentration preheating furnace
Material.
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| CN201910410951.9A CN110127611A (en) | 2019-05-16 | 2019-05-16 | Ammonia synthesis process raw material gas shift heating system |
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| CN201910410951.9A CN110127611A (en) | 2019-05-16 | 2019-05-16 | Ammonia synthesis process raw material gas shift heating system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113526525A (en) * | 2021-06-29 | 2021-10-22 | 福州大学化肥催化剂国家工程研究中心 | Synthetic ammonia tower and renewable energy source synthetic ammonia system with waste heat step recovery |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113526525A (en) * | 2021-06-29 | 2021-10-22 | 福州大学化肥催化剂国家工程研究中心 | Synthetic ammonia tower and renewable energy source synthetic ammonia system with waste heat step recovery |
| CN113526525B (en) * | 2021-06-29 | 2022-09-02 | 福州大学化肥催化剂国家工程研究中心 | Synthetic ammonia tower and renewable energy source synthetic ammonia system with waste heat step recovery |
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