CN117582903A - Synthetic ammonia system based on single compressor - Google Patents
Synthetic ammonia system based on single compressor Download PDFInfo
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- CN117582903A CN117582903A CN202311504994.6A CN202311504994A CN117582903A CN 117582903 A CN117582903 A CN 117582903A CN 202311504994 A CN202311504994 A CN 202311504994A CN 117582903 A CN117582903 A CN 117582903A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 174
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 87
- 239000007789 gas Substances 0.000 claims abstract description 140
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 67
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 60
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 42
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 18
- 239000003507 refrigerant Substances 0.000 claims abstract description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims description 39
- 238000000926 separation method Methods 0.000 claims description 38
- 239000002918 waste heat Substances 0.000 claims description 22
- 238000011084 recovery Methods 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 12
- 150000002431 hydrogen Chemical class 0.000 claims description 12
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 238000007710 freezing Methods 0.000 claims description 4
- 230000008014 freezing Effects 0.000 claims description 4
- 239000006227 byproduct Substances 0.000 claims description 3
- 239000002994 raw material Substances 0.000 abstract description 7
- 230000001276 controlling effect Effects 0.000 description 18
- 230000002194 synthesizing effect Effects 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
Classifications
-
- 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
- C01C1/0482—Process control; Start-up or cooling-down procedures
-
- 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
-
- 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
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/008—Feed or outlet control devices
-
- 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
- C01C1/0447—Apparatus other than synthesis reactors
- C01C1/0452—Heat exchangers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/02—Pipe-line systems for gases or vapours
- F17D1/065—Arrangements for producing propulsion of gases or vapours
- F17D1/07—Arrangements for producing propulsion of gases or vapours by compression
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
-
- 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
- B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
- B01J2204/002—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the feeding side being of particular interest
-
- 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
- B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
- B01J2204/007—Aspects relating to the heat-exchange of the feed or outlet devices
-
- 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)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Automation & Control Theory (AREA)
- Combustion & Propulsion (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a synthetic ammonia system based on a single compressor, and relates to the technical field of nitrogen and hydrogen synthetic ammonia. The invention comprises a compressor, wherein the air outlet of the compressor is communicated with a heat exchanger A, the refrigerant outlet of the heat exchanger A is respectively communicated with a first pipeline, a second pipeline and a third pipeline through pipelines, and the second pipeline and the third pipeline are respectively provided with a heat exchanger B and a heat exchanger C; a temperature sensor A is arranged on the pipeline; the first pipeline, the second pipeline and the third pipeline are all connected to the air inlet of the ammonia synthesis tower. According to the invention, the three pipelines are arranged at the outlet end of the compressor to be communicated with the ammonia synthesis tower, and the temperature sensor A is arranged, so that when the ammonia synthesis tower is used, control gas passes through the compressor and then selectively passes through at least one of the three pipelines to enter the ammonia synthesis tower, secondary temperature control is conveniently carried out on raw material gas entering the ammonia synthesis tower, the accuracy and precision of temperature control are improved, and the raw material gas entering the ammonia synthesis tower is controlled to be within a set temperature range under any condition.
Description
Technical Field
The invention belongs to the technical field of nitrogen and hydrogen synthesis ammonia, and particularly relates to a synthesis ammonia system based on a single compressor.
Background
Under certain conditions, the hydrogen and the nitrogen can be synthesized into ammonia, the ammonia synthesis process belongs to a gas-solid catalyst reaction process, the reaction is carried out under higher pressure, and from the aspect of ammonia synthesis reaction kinetics, the ammonia synthesis reaction is a heterogeneous gas catalytic reaction, and the ammonia generation speed can be accelerated by increasing the pressure, so that the ammonia content in the gas is rapidly increased; second, the rate of chemical reaction of ammonia synthesis reaction increases significantly with increasing temperature. It is therefore desirable to have the ammonia synthesis reaction run as technically possible at the optimum reaction temperature for greater throughput and higher ammonia synthesis efficiency.
Therefore, in order to ensure that the ammonia synthesis reaction proceeds as much as possible at the optimum reaction temperature, it is necessary to heat the raw material gas fed into the ammonia synthesis column.
As in CN105731493A, a method for low H is disclosed 2 /N 2 Process for producing synthetic ammonia from synthesis gas comprising reacting a sub-stoichiometric ratio of H 2 -N 2 Mixing the synthesis gas with the circulating synthesis gas, pressurizing by a compressor and preheating by a heat exchanger; since the amount of the mixed gas discharged through the synthesis tower and the amount of the raw gas supplied into the synthesis tower through the compressor are fluctuated in actual production, in practice, the mixed gas and the raw gas are subjected to heat exchange by the heat exchanger to heat the raw gas entering the synthesis tower, the temperature difference after the raw gas is heated is large in practice, and in the actual production process, the temperature difference fluctuation of the raw gas is large, so that the ammonia synthesis reaction temperature is fluctuated greatly, and the ammonia synthesis reaction can not be well realized at the optimal reaction temperature all the time.
Disclosure of Invention
The invention aims to provide a synthetic ammonia system based on a single compressor, which is characterized in that three pipelines are arranged at the outlet end of the compressor to be communicated with an ammonia synthesis tower, and a temperature sensor A is arranged, so that when the synthetic ammonia system is used, control gas passes through the compressor and then selectively passes through at least one of the three pipelines to enter the ammonia synthesis tower, secondary temperature control is conveniently carried out on raw material gas entering the ammonia synthesis tower, and the problem of large temperature difference fluctuation of the raw material gas entering the synthesis tower in the prior art is solved.
In order to solve the technical problems, the invention is realized by the following technical scheme:
the invention relates to an ammonia synthesis system based on a single compressor, which comprises a compressor, wherein an air inlet of the compressor is communicated with a three-way proportional valve A, and two inlet ends of the three-way proportional valve A are respectively communicated with a cooling separation assembly and a hydrogen-nitrogen supply assembly; the air outlet of the compressor is communicated with a heat exchanger A, the refrigerant outlet of the heat exchanger A is respectively communicated with a first pipeline, a second pipeline and a third pipeline through pipelines, and a first valve, a second valve and a third valve are respectively arranged on the first pipeline, the second pipeline and the third pipeline; the second pipeline and the third pipeline are respectively provided with a heat exchanger B and a heat exchanger C; the heat source inlet of the heat exchanger C is communicated with the heat source outlet of the heat exchanger A, and the heat source outlet of the heat exchanger C is communicated with the cooling separation assembly; the cold source inlet of the heat exchanger B is communicated with a refrigerant supply unit; a temperature sensor A is arranged on the pipeline; the first pipeline, the second pipeline and the third pipeline are all connected to the air inlet of the ammonia synthesis tower; the gas outlet of the ammonia synthesis tower is communicated with a waste heat recovery unit, and the gas outlet end of the waste heat recovery unit is communicated with a heat source inlet of the heat exchanger A.
Further, the waste heat recovery unit selects a waste heat boiler, and tower gas from the ammonia synthesis tower enters the waste heat boiler to produce a byproduct of 1.2MPaG saturated steam; the saturated steam enters the heat exchanger A to exchange heat with the gas entering the tower, and the temperature is reduced to 70-80 ℃.
As a preferable technical scheme of the invention, the compressor is a multistage reciprocating compressor, the hydrogen-nitrogen supply assembly comprises a nitrogen tank and a hydrogen tank, and the cooling separation assembly comprises a water cooler, a cold exchanger, an ammonia cooler, an ammonia separator and a freezing section.
The method for synthesizing ammonia comprises the following steps:
stp1, delivering hydrogen, nitrogen and recovered gas into a heat exchanger A through a compressor, and heating by using tower outlet gas;
stp2, judging whether the gas entering the tower meets the set temperature or not through a temperature sensor A; if the gas entering the tower meets the set temperature, the first valve is controlled to be opened, and the second valve and the third valve are controlled to be closed;
if the tower inlet gas is higher than the set temperature, the second valve is controlled to be opened, and the first valve and the third valve are controlled to be closed;
and if the tower inlet gas is lower than the set temperature, controlling the third valve to open and close the second valve and the first valve.
As a preferable technical scheme of the invention, a three-way proportional valve B is arranged on a pipeline between the waste heat recovery unit and the heat exchanger A, and one air outlet end of the three-way proportional valve B is communicated with the cooling separation assembly.
The method for synthesizing ammonia comprises the following steps:
stp1, delivering hydrogen, nitrogen and recovered gas into a heat exchanger A through a compressor, and heating by using tower outlet gas;
stp2, judging whether the gas entering the tower meets the set temperature or not through a temperature sensor A; if the gas entering the tower meets the set temperature, the first valve is controlled to be opened, and the second valve and the third valve are controlled to be closed;
if the gas entering the tower is higher than the set temperature, the proportion of the gas flowing into the cooling separation assembly and the heat exchanger A is increased through the three-way proportional valve B;
if the gas entering the tower is lower than the set temperature, the proportion of the gas flowing into the cooling separation assembly and the heat exchanger A is reduced through the three-way proportional valve B.
As a preferable technical scheme of the invention, a fourth pipeline is communicated between the heat exchanger A and the heat exchanger C, a fifth pipeline is communicated between the heat exchanger C and the cooling separation assembly, and a branch pipe is communicated between the fourth pipeline and the fifth pipeline; and a fourth valve and a fifth valve are respectively arranged on the fourth pipeline and the branch pipe.
The method for synthesizing ammonia comprises the following steps:
stp1, delivering hydrogen, nitrogen and recovered gas into a heat exchanger A through a compressor, and heating by using tower outlet gas;
stp2, judging whether the gas entering the tower meets the set temperature or not through a temperature sensor A; if the gas entering the tower meets the set temperature, the first valve is controlled to be opened, and the second valve and the third valve are controlled to be closed;
if the gas entering the tower is higher than the set temperature; controlling the second valve to open and closing the first valve and the third valve;
if the gas entering the tower is lower than the set temperature; the third valve is controlled to open and close the second valve and the first valve, and the air flow ratio of the heat exchanger a to the heat exchanger C and the cooling separation assembly is adjusted by controlling the fourth valve and the fifth valve according to the actual temperature difference.
As a preferable technical scheme of the invention, a fourth pipeline is communicated between the heat exchanger A and the heat exchanger C, a fifth pipeline is communicated between the heat exchanger C and the cooling separation assembly, and a branch pipe is communicated between the fourth pipeline and the fifth pipeline; a fourth valve and a fifth valve are respectively arranged on the fourth pipeline and the branch pipe; and a three-way proportional valve B is arranged on a pipeline between the waste heat recovery unit and the heat exchanger A, and one air outlet end of the three-way proportional valve B is communicated with the cooling separation assembly.
The method for synthesizing ammonia comprises the following steps:
stp1, delivering hydrogen, nitrogen and recovered gas into a heat exchanger A through a compressor, and heating by using tower outlet gas;
stp2, judging whether the gas entering the tower meets the set temperature or not through a temperature sensor A; if the gas entering the tower meets the set temperature, the first valve is controlled to be opened, and the second valve and the third valve are controlled to be closed;
if the gas entering the tower is higher than the set temperature, the second valve is controlled to be opened and the first valve and the third valve are controlled to be closed, or the proportion of the gas flow entering the cooling separation assembly and the heat exchanger A is increased through the three-way proportional valve B;
if the gas entering the tower is lower than the set temperature, the proportion of the gas flowing into the cooling separation assembly and the heat exchanger A is reduced through the three-way proportional valve B, or the third valve is controlled to be opened, the second valve and the first valve are closed, and meanwhile, the proportion of the gas flowing into the heat exchanger C and the cooling separation assembly through the heat exchanger A is adjusted through the fourth valve and the fifth valve according to the actual temperature difference.
The invention has the following beneficial effects:
according to the invention, the three pipelines are arranged at the outlet end of the compressor to be communicated with the ammonia synthesis tower, and the temperature sensor A is arranged, so that when the ammonia synthesis tower is used, the control gas passes through the compressor and then selectively passes through at least one of the three pipelines to enter the ammonia synthesis tower, the secondary temperature control of the raw material gas entering the ammonia synthesis tower is facilitated, the accuracy and precision of temperature control are improved, and the raw material gas entering the ammonia synthesis tower is controlled to be within a set temperature range under any condition.
Of course, it is not necessary for any one product to practice the invention to achieve all of the advantages set forth above at the same time.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed for the description of the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a block diagram of an ammonia synthesis system according to example 1 of the present invention;
FIG. 2 is a block diagram of an ammonia synthesis system according to example 2 of the present invention;
FIG. 3 is a block diagram of an ammonia synthesis system according to example 3 of the present invention;
FIG. 4 is a block diagram of an ammonia synthesis system according to example 4 of the present invention;
FIG. 5 is a block diagram of an ammonia synthesis system according to example 5 of the present invention.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Embodiment 1, as shown in FIG. 1, a synthetic ammonia system based on a single compressor comprises a compressor 1, an air inlet of which is communicated with a three-way proportional valve A10, two inlet ends of the three-way proportional valve A10 are respectively communicated with a water cooler and a hydrogen-nitrogen supply assembly 3; meanwhile, the air outlet of the compressor 1 is communicated with the heat exchanger A4;
the hydrogen-nitrogen supply assembly 3 comprises a nitrogen tank and a hydrogen tank, the tail end of the water cooler is sequentially communicated with the cold exchanger, the ammonia cooler, the ammonia separator and the freezing section, and the water cooler, the cold exchanger, the ammonia cooler, the ammonia separator and the freezing section jointly form a cooling separation assembly 2;
the gas outlet of the ammonia synthesis tower 5 is communicated with a waste heat recovery unit 6, and the gas outlet end of the waste heat recovery unit 6 is communicated with a heat source inlet of the heat exchanger A4;
in the present invention, three sets of temperature adjustment pipes are provided for temperature control of the raw gas controlled to enter the ammonia synthesis tower 5, respectively;
specifically, the device comprises a first pipeline 40, a second pipeline 41 and a third pipeline 42 which are respectively communicated with a pipeline, wherein the pipeline is communicated with a refrigerant outlet of a heat exchanger A4, and a temperature sensor A400 is arranged on the pipeline; the second pipeline 41 and the third pipeline 42 are respectively provided with a heat exchanger B411 and a heat exchanger C421, and the first pipeline 40, the second pipeline 41 and the third pipeline 42 are respectively provided with a first valve 401, a second valve 412 and a third valve 422; and the first pipeline 40, the second pipeline 41 and the third pipeline 42 are all communicated with the air inlet of the ammonia synthesis tower 5;
the method for synthesizing ammonia comprises the following steps:
stp1, the hydrogen, the nitrogen and the recovered gas are sent into a heat exchanger A4 together through a compressor 1, and the tower outlet gas is adopted for heating;
stp2, judging whether the gas entering the tower meets the set temperature through a temperature sensor A400; if the tower entering gas meets the set temperature, the first valve 401 is controlled to be opened and the second valve 412 and the third valve 422 are controlled to be closed;
if the tower inlet gas is higher than the set temperature, the second valve 412 is controlled to open and close the first valve 401 and the third valve 422;
if the incoming gas is below the set temperature, the third valve 422 is controlled to open and close the second valve 412 and the first valve 401.
In the above, the difference between the temperature of the gas entering the tower and the set temperature is determined to be adjusted;
on the basis, the heat source inlet of the heat exchanger C421 is communicated with the heat source outlet of the heat exchanger A4, and the heat source outlet of the heat exchanger C421 is communicated with the cooling separation assembly 2; the cold source inlet of the heat exchanger B411 is communicated with a refrigerant supply unit;
in the above Stp2, the temperature can be controlled by controlling the flow rate of the refrigerant supplied into the heat exchanger B411 by the refrigerant supply means; the second valve 412 is opened while the first valve 401 is kept open, and the temperature is controlled by controlling the other flow ratio of the compressor 1 through the second valve 412 and the first valve 401.
In Stp2, the temperature of the tower inlet gas can be raised secondarily through the heat exchanger C421; also in the above, or while the third valve 422 is opened, the first valve 401 is kept open, and the temperature is controlled by controlling the other flow ratio of the compressor 1 through the third valve 422 and the first valve 401.
It can be understood that the waste heat recovery unit 6 in the invention adopts a waste heat boiler, and the tower gas from the ammonia synthesis tower 5 enters the waste heat boiler to produce a byproduct of 1.2MPaG saturated steam; the saturated steam enters the heat exchanger A4 to exchange heat with the gas entering the tower, the temperature is reduced to 70-80 ℃, and the compressor 1 is a multistage reciprocating compressor.
In example 1, when the set temperature is 170-180 ℃;
at this time, when the temperature sensor A400 detects that the gas problem is 150 ℃, the third valve 422 is opened, the second valve 412 and the first valve 401 are closed, and the heat exchanger C421 is utilized to perform secondary temperature rise on the tower inlet gas; when a gas problem of 160 ℃ is detected by the temperature sensor a400, the third valve 422 is opened at this time, the first valve 401 is kept open, and the flow ratio of the gas passing through the third valve 422 and the first valve 401 by controlling the compressor 1 is 1:1.
at this time, when the temperature sensor A400 detects that the gas problem is 200 ℃, the second valve 412 is controlled to be opened and the first valve 401 and the third valve 422 are closed, and the heat exchanger B411 is used for cooling the tower entering gas; when a gas problem of 190 ℃ is detected by the temperature sensor a400, the second valve 412 is opened at this time, while the first valve 401 is kept open, and the flow ratio of the gas passing through the second valve 412 and the first valve 401 by controlling the compressor 1 is 1:1.
example 2, as shown in fig. 2, is based on example 1; a three-way proportional valve B61 is arranged on a pipeline between the waste heat recovery unit 6 and the heat exchanger A4, and one air outlet end of the three-way proportional valve B61 is communicated with the cooling separation assembly 2.
The method for synthesizing ammonia comprises the following steps:
stp1, the hydrogen, the nitrogen and the recovered gas are sent into a heat exchanger A4 together through a compressor 1, and the tower outlet gas is adopted for heating;
stp2, judging whether the gas entering the tower meets the set temperature through a temperature sensor A400; if the tower entering gas meets the set temperature, the first valve 401 is controlled to be opened and the second valve 412 and the third valve 422 are controlled to be closed;
if the gas entering the tower is higher than the set temperature, the proportion of the gas flowing into the cooling separation assembly 2 and the heat exchanger A4 is increased through the three-way proportional valve B61;
if the incoming gas is below the set temperature, the ratio of the gas flows to the cooling separation assembly 2 and the heat exchanger A4 is reduced by the three-way proportional valve B61.
It can be appreciated that in the above, the adjustment is performed by determining the difference between the temperature of the incoming gas and the set temperature;
in the above Stp2, the temperature can be controlled by controlling the flow rate of the refrigerant supplied into the heat exchanger B411 by the refrigerant supply means; the second valve 412 is opened while the first valve 401 is kept open, and the temperature is controlled by controlling the other flow ratio of the compressor 1 through the second valve 412 and the first valve 401.
In Stp2, the temperature of the tower inlet gas can be raised secondarily through the heat exchanger C421; also in the above, or while the third valve 422 is opened, the first valve 401 is kept open, and the temperature is controlled by controlling the other flow ratio of the compressor 1 through the third valve 422 and the first valve 401.
Embodiment 3, as shown in fig. 3, on the basis of embodiment 1, a fourth pipeline 43 is communicated between the heat exchanger A4 and the heat exchanger C421, a fifth pipeline 45 is communicated between the heat exchanger C421 and the cooling separation assembly 2, and a branch pipe 44 is communicated between the fourth pipeline 43 and the fifth pipeline 45; a fourth valve 431 and a fifth valve 441 are provided on the fourth pipe 43 and the branch pipe 44, respectively.
The method for synthesizing ammonia comprises the following steps:
stp1, the hydrogen, the nitrogen and the recovered gas are sent into a heat exchanger A4 together through a compressor 1, and the tower outlet gas is adopted for heating;
stp2, judging whether the gas entering the tower meets the set temperature through a temperature sensor A400; if the tower entering gas meets the set temperature, the first valve 401 is controlled to be opened and the second valve 412 and the third valve 422 are controlled to be closed;
if the gas entering the tower is higher than the set temperature; the second valve 412 is controlled to open and close the first valve 401 and the third valve 422;
if the gas entering the tower is lower than the set temperature; the third valve 422 is controlled to open and close the second valve 412 and the first valve 401 while the ratio of the air flow of the heat exchanger A4 to the heat exchanger C421 and the cooling separation assembly 2 is adjusted by controlling the fourth valve 431 and the fifth valve 441 according to the actual temperature difference.
In the above Stp2, the temperature can be controlled by controlling the flow rate of the refrigerant supplied into the heat exchanger B411 by the refrigerant supply means; the second valve 412 is opened while the first valve 401 is kept open, and the temperature is controlled by controlling the other flow ratio of the compressor 1 through the second valve 412 and the first valve 401.
In Stp2, the temperature of the tower inlet gas can be raised secondarily through the heat exchanger C421; also in the above, or while the third valve 422 is opened, the first valve 401 is kept open, and the temperature is controlled by controlling the other flow ratio of the compressor 1 through the third valve 422 and the first valve 401.
Embodiment 3, as shown in fig. 3, on the basis of embodiment 1, a fourth pipeline 43 is communicated between the heat exchanger A4 and the heat exchanger C421, a fifth pipeline 45 is communicated between the heat exchanger C421 and the cooling separation assembly 2, and a branch pipe 44 is communicated between the fourth pipeline 43 and the fifth pipeline 45; a fourth valve 431 and a fifth valve 441 are respectively arranged on the fourth pipeline 43 and the branch pipe 44; a three-way proportional valve B61 is arranged on a pipeline between the waste heat recovery unit 6 and the heat exchanger A4, and one air outlet end of the three-way proportional valve B61 is communicated with the cooling separation assembly 2.
The method for synthesizing ammonia comprises the following steps:
stp1, the hydrogen, the nitrogen and the recovered gas are sent into a heat exchanger A4 together through a compressor 1, and the tower outlet gas is adopted for heating;
stp2, judging whether the gas entering the tower meets the set temperature through a temperature sensor A400; if the tower entering gas meets the set temperature, the first valve 401 is controlled to be opened and the second valve 412 and the third valve 422 are controlled to be closed;
if the tower inlet gas is higher than the set temperature, the second valve 412 is controlled to open and close the first valve 401 and the third valve 422, or the proportion of the gas flow which is introduced into the cooling separation assembly 2 and the heat exchanger A4 is increased through the three-way proportional valve B61;
if the tower inlet gas is lower than the set temperature, the three-way proportional valve B61 is used for reducing the gas flow ratio of the cooling separation assembly 2 to the heat exchanger A4, or the third valve 422 is controlled to be opened and the second valve 412 and the first valve 401 are controlled to be closed, and meanwhile, the fourth valve 431 and the fifth valve 441 are controlled to adjust the gas flow ratio of the heat exchanger A4 to the heat exchanger C421 and the cooling separation assembly 2 according to the actual temperature difference.
In the above Stp2, the temperature can be controlled by controlling the flow rate of the refrigerant supplied into the heat exchanger B411 by the refrigerant supply means; the second valve 412 is opened while the first valve 401 is kept open, and the temperature is controlled by controlling the other flow ratio of the compressor 1 through the second valve 412 and the first valve 401.
In Stp2, the temperature of the tower inlet gas can be raised secondarily through the heat exchanger C421; also in the above, or while the third valve 422 is opened, the first valve 401 is kept open, and the temperature is controlled by controlling the other flow ratio of the compressor 1 through the third valve 422 and the first valve 401.
Example 5 as shown in fig. 5, it will be appreciated that in some possible embodiments, a temperature control module 7 may be disposed on the pipeline between the heat recovery unit 6 and the heat exchanger A4, or the temperature control module 7 may be used to replace the heat recovery unit 6, so as to regulate the temperature of the exhaust gas entering the heat exchanger A4.
In one possible embodiment, the temperature control module 7 is a gas cooler.
In another possible embodiment, as shown in fig. 5, the temperature control module 7 includes a mixer 70, where two air inlet connectors 71 are provided at one end of the mixer 70 and an air outlet connector 72 is provided at the other end; the air outlet joint 72 is communicated with the air inlet of the heat exchanger A4, one air inlet joint 71 introduces tail gas from the air outlet of the ammonia synthesis tower 5 or the waste heat recovery unit 6, and the other air inlet joint 71 introduces room temperature air;
and a temperature sensor B is arranged in the mixer 70 near the air outlet joint 72, and by arranging the temperature sensor B, on the premise of ensuring that the amount of the air introduced from the air outlet of the ammonia synthesis tower 5 is unchanged, the temperature of the air discharged from the mixer 70 is adjusted by adjusting the amount of the air introduced from the air inlet joint 71 by the mixer 70 due to the change of the room temperature or the exhaust temperature of the ammonia synthesis tower 5. The temperature of the gas entering the heat exchanger A4 is regulated to be stable, the temperature of the gas which is output through heat exchange of the heat exchanger A4 is further controlled to be stable, and the temperature of the mixed gas entering the ammonia synthesis tower 5 is regulated through three groups of temperature regulating pipelines conveniently.
In the description of the present specification, the descriptions of the terms "one embodiment," "example," "specific example," and the like, mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms do not necessarily refer to the same embodiments or examples. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The preferred embodiments of the invention disclosed above are intended only to assist in the explanation of the invention. The preferred embodiments are not exhaustive or to limit the invention to the precise form disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best understand and utilize the invention. The invention is limited only by the claims and the full scope and equivalents thereof.
Claims (10)
1. An ammonia synthesis system based on a single compressor, characterized in that: the device comprises a compressor (1) with an air inlet communicated with a three-way proportional valve A (10), wherein two inlet ends of the three-way proportional valve A (10) are respectively communicated with a cooling separation assembly (2) and a hydrogen-nitrogen supply assembly (3);
the air outlet of the compressor (1) is communicated with the heat exchanger A (4), the refrigerant outlet of the heat exchanger A (4) is communicated with a first pipeline (40), a second pipeline (41) and a third pipeline (42) through pipelines respectively, and a first valve (401), a second valve (412) and a third valve (422) are respectively arranged on the first pipeline (40), the second pipeline (41) and the third pipeline (42);
the second pipeline (41) and the third pipeline (42) are respectively provided with a heat exchanger B (411) and a heat exchanger C (421);
the heat source inlet of the heat exchanger C (421) is communicated with the heat source outlet of the heat exchanger A (4), and the heat source outlet of the heat exchanger C (421) is communicated with the cooling separation assembly (2);
a cold source inlet of the heat exchanger B (411) is communicated with a refrigerant supply unit;
and a temperature sensor A (400) is arranged on the pipeline;
the first pipeline (40), the second pipeline (41) and the third pipeline (42) are all connected to the air inlet of the ammonia synthesis tower (5); the gas outlet of the ammonia synthesis tower (5) is communicated with the waste heat recovery unit (6), and the gas outlet end of the waste heat recovery unit (6) is communicated with the heat source inlet of the heat exchanger A (4).
2. The ammonia synthesis system based on a single compressor according to claim 1, wherein the waste heat recovery unit (6) is a waste heat boiler, and tower gas from the ammonia synthesis tower (5) enters the waste heat boiler to produce 1.2MPaG saturated steam as a byproduct; the saturated steam enters the heat exchanger A (4) to exchange heat with the gas entering the tower, and the temperature is reduced to 70-80 ℃. .
3. A synthesis ammonia system based on a single compressor according to claim 1, wherein the compressor (1) is a multistage reciprocating compressor, the hydrogen-nitrogen supply assembly (3) comprises a nitrogen tank and a hydrogen tank, and the cooling separation assembly (2) comprises a water cooler, a cold exchanger, an ammonia cooler, an ammonia separator and a freezing section.
4. A single compressor-based ammonia synthesis system according to any one of claims 1-3, wherein the ammonia synthesis process comprises:
stp1, hydrogen, nitrogen and recovered gas are sent into a heat exchanger A (4) together through a compressor (1), and tower outlet gas is adopted for heating;
stp2, judging whether the tower inlet gas meets the set temperature through a temperature sensor A (400); if the tower entering gas meets the set temperature, controlling the first valve (401) to open and close the second valve (412) and the third valve (422);
if the tower inlet gas is higher than the set temperature, the second valve (412) is controlled to be opened, and the first valve (401) and the third valve (422) are controlled to be closed;
if the incoming gas is below the set temperature, the third valve (422) is controlled to open and close the second valve (412) and the first valve (401).
5. A single compressor based ammonia synthesis system according to any one of claims 1-3, wherein a three-way proportional valve B (61) is arranged in the pipeline between the waste heat recovery unit (6) and the heat exchanger a (4), and an outlet end of the three-way proportional valve B (61) is connected to the cooling separation assembly (2).
6. The single compressor-based ammonia synthesis system of claim 5, wherein the ammonia synthesis process comprises:
stp1, hydrogen, nitrogen and recovered gas are sent into a heat exchanger A (4) together through a compressor (1), and tower outlet gas is adopted for heating;
stp2, judging whether the tower inlet gas meets the set temperature through a temperature sensor A (400); if the tower entering gas meets the set temperature, controlling the first valve (401) to open and close the second valve (412) and the third valve (422);
if the gas entering the tower is higher than the set temperature, the proportion of the gas flowing into the cooling separation assembly (2) and the heat exchanger A (4) is increased through the three-way proportional valve B (61);
if the gas entering the tower is lower than the set temperature, the proportion of the gas flow entering the cooling separation assembly (2) and the heat exchanger A (4) is reduced through the three-way proportional valve B (61).
7. A single compressor-based ammonia synthesis system according to any one of claims 1-3, wherein a fourth line (43) is connected between the heat exchanger a (4) and the heat exchanger C (421), a fifth line (45) is connected between the heat exchanger C (421) and the cooling separation unit (2), and a branch line (44) is connected between the fourth line (43) and the fifth line (45);
a fourth valve (431) and a fifth valve (441) are respectively arranged on the fourth pipeline (43) and the branch pipe (44).
8. The single compressor-based ammonia synthesis system of claim 7, wherein the ammonia synthesis process comprises:
stp1, hydrogen, nitrogen and recovered gas are sent into a heat exchanger A (4) together through a compressor (1), and tower outlet gas is adopted for heating;
stp2, judging whether the tower inlet gas meets the set temperature through a temperature sensor A (400); if the tower entering gas meets the set temperature, controlling the first valve (401) to open and close the second valve (412) and the third valve (422);
if the gas entering the tower is higher than the set temperature; controlling the second valve (412) to open and close the first valve (401) and the third valve (422);
if the gas entering the tower is lower than the set temperature; the third valve (422) is controlled to open and close the second valve (412) and the first valve (401), while the ratio of the air flow to the heat exchanger C (421) and the cooling separation assembly (2) of the heat exchanger a (4) is adjusted by controlling the fourth valve (431) and the fifth valve (441) according to the actual temperature difference.
9. A single compressor-based ammonia synthesis system according to any one of claims 1-3, wherein a fourth line (43) is connected between the heat exchanger a (4) and the heat exchanger C (421), a fifth line (45) is connected between the heat exchanger C (421) and the cooling separation unit (2), and a branch line (44) is connected between the fourth line (43) and the fifth line (45); a fourth valve (431) and a fifth valve (441) are respectively arranged on the fourth pipeline (43) and the branch pipe (44);
a three-way proportional valve B (61) is arranged on a pipeline between the waste heat recovery unit (6) and the heat exchanger A (4), and one air outlet end of the three-way proportional valve B (61) is connected with the cooling separation assembly (2).
10. The single compressor-based ammonia synthesis system of claim 9, wherein the ammonia synthesis process comprises:
stp1, hydrogen, nitrogen and recovered gas are sent into a heat exchanger A (4) together through a compressor (1), and tower outlet gas is adopted for heating;
stp2, judging whether the tower inlet gas meets the set temperature through a temperature sensor A (400); if the tower entering gas meets the set temperature, controlling the first valve (401) to open and close the second valve (412) and the third valve (422);
if the tower inlet gas is higher than the set temperature, the second valve (412) is controlled to be opened and the first valve (401) and the third valve (422) are controlled to be closed, or the proportion of the gas flow which is introduced into the cooling separation assembly (2) and the heat exchanger A (4) is increased through the three-way proportional valve B (61);
if the tower inlet gas is lower than the set temperature, the air flow ratio of the cooling separation assembly (2) to the heat exchanger A (4) is reduced through the three-way proportional valve B (61), or the third valve (422) is controlled to be opened and the second valve (412) and the first valve (401) are controlled to be closed, and meanwhile, the air flow ratio of the heat exchanger A (4) to the heat exchanger C (421) and the cooling separation assembly (2) is adjusted through controlling the fourth valve (431) and the fifth valve (441) according to the actual temperature difference.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311504994.6A CN117582903A (en) | 2023-11-13 | 2023-11-13 | Synthetic ammonia system based on single compressor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311504994.6A CN117582903A (en) | 2023-11-13 | 2023-11-13 | Synthetic ammonia system based on single compressor |
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| CN117582903A true CN117582903A (en) | 2024-02-23 |
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| CN202311504994.6A Pending CN117582903A (en) | 2023-11-13 | 2023-11-13 | Synthetic ammonia system based on single compressor |
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| CN (1) | CN117582903A (en) |
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