CN217868148U - Hydrogen recovery pressure energy and gas comprehensive utilization system - Google Patents
Hydrogen recovery pressure energy and gas comprehensive utilization system Download PDFInfo
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- CN217868148U CN217868148U CN202221953229.3U CN202221953229U CN217868148U CN 217868148 U CN217868148 U CN 217868148U CN 202221953229 U CN202221953229 U CN 202221953229U CN 217868148 U CN217868148 U CN 217868148U
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- 239000007789 gas Substances 0.000 title claims abstract description 109
- 239000001257 hydrogen Substances 0.000 title claims abstract description 17
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 17
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 16
- 238000011084 recovery Methods 0.000 title claims abstract description 13
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 115
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 60
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 59
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 54
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000001035 drying Methods 0.000 claims abstract description 40
- 239000002808 molecular sieve Substances 0.000 claims abstract description 40
- 230000008929 regeneration Effects 0.000 claims abstract description 25
- 238000011069 regeneration method Methods 0.000 claims abstract description 25
- 239000012528 membrane Substances 0.000 claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 238000005406 washing Methods 0.000 claims description 19
- 238000000746 purification Methods 0.000 claims description 14
- 230000001172 regenerating effect Effects 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 5
- 239000012466 permeate Substances 0.000 abstract description 3
- 150000002431 hydrogen Chemical class 0.000 abstract 1
- 238000005201 scrubbing Methods 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 51
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 20
- 238000001179 sorption measurement Methods 0.000 description 15
- 239000007788 liquid Substances 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 230000006837 decompression Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Images
Classifications
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- 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
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- Drying Of Gases (AREA)
Abstract
The utility model relates to a gaseous optimal utilization is retrieved to synthetic ammonia unloading embrane method hydrogen, specifically is a hydrogen recovery pressure energy and gaseous integrated utilization system, and the entry of operation drying tower links to each other with the export of scrubbing tower, the export of operation drying tower links to each other with the entry of membrane separator, the permeate gas export of membrane separator links to each other with the entry of regeneration molecular sieve, and the exit linkage of regeneration molecular sieve is to one section synthetic gas compressor entrance, the non-permeate gas exit linkage of membrane separator is to the entry of expander, and the exit linkage of expander is to the cold side entry of heat exchanger, and the cold side exit linkage of heat exchanger is to the cold side entry of heater, and the cold side exit linkage of heater is to the entry of regeneration drying tower. The non-permeable gas of the membrane separator in the utility model is decompressed by the expander to recover the pressure energy of the non-permeable gas; and exchanging heat between the low-temperature gas expanded by the expander and the gas ammonia of the ammonia synthesis system to recover cold.
Description
Technical Field
The utility model relates to a gaseous optimal utilization field, specifically a hydrogen recovery pressure energy and gaseous comprehensive utilization system are retrieved to synthetic ammonia unloading embrane method hydrogen.
Background
In the existing ammonia synthesis plant, as shown in fig. 1, the decarbonized gas from the previous section is compressed by a first-stage synthesis gas compressor 1, enters a double-stage methane purification system 2 for purification, and most of the CO and CO are purified 2 The gas is converted into methanol and methane, the methanol and the methane are cooled and separated and then enter a molecular sieve drying system, the adsorption and drying of the molecular sieve are realized by utilizing the principle that the adsorption capacity of an adsorbent to the gas changes along with different adsorption pressures and temperatures, one adsorption tower is used as an operation molecular sieve 3 to carry out high-pressure low-temperature adsorption, the other adsorption tower is used as a regeneration molecular sieve 4 to carry out decompression heating regeneration, and the two adsorption towers are alternately used to realize continuous drying of the gas. Fresh gas H dried by running molecular sieve 3 2 、N 2 Most of the ammonia is compressed by a two-stage synthesis gas compressor 5 and is supplemented into a synthesis ammonia system 6 for synthesis gas ammonia; and a small part of gas is subjected to pressure reduction and heating to be used for regenerating the regenerated molecular sieve 4, and then returns to the synthesis gas compressor 1 again to be subjected to cyclic compression, so that the effective work of the synthesis gas compressor is wasted. Tail gas of the ammonia synthesis system 6 is washed by a water washing tower 7 to remove ammonia gas, enters a heater 8 to raise the temperature, then enters a membrane separator 9 to recover hydrogen by adopting a semi-permeable membrane method, and the permeation gas hydrogen passing through the membrane separator returns to an inlet of a first section of synthesis gas compressor 1 to be recycled; the non-permeable gas is sent to other working sections after being depressurized by the pressure reducing valve 10, so that great energy waste exists, and the on-site pressure reducing valve 10 is loud in noise.
SUMMERY OF THE UTILITY MODEL
The utility model discloses a solve a large amount of energies when retrieving the inflation decompression of non-permeability gas, also provide a hydrogen recovery pressure energy and gaseous comprehensive utilization system for the acting that reduces the compressor simultaneously.
The utility model discloses a realize through following technical scheme: a hydrogen recovery pressure energy and gas comprehensive utilization system comprises a first-stage synthesis gas compressor, a double-stage purification system, an operation molecular sieve, a regeneration molecular sieve, a second-stage synthesis gas compressor, a synthesis ammonia system, a water washing tower, a heater and a membrane separator;
the system comprises a first section of synthesis gas compressor, a double-stage purification system, a running molecular sieve, a second section of synthesis gas compressor, a synthetic ammonia system and a water washing tower, wherein the first section of synthesis gas compressor, the double-stage purification system, the running molecular sieve, the second section of synthesis gas compressor, the synthetic ammonia system and the water washing tower are sequentially connected, an inlet of the running drying tower is connected with an outlet of the water washing tower, an outlet of the running drying tower is connected with an inlet of a membrane separator, a permeation gas outlet of the membrane separator is connected with an inlet of a regenerated molecular sieve, an outlet of the regenerated molecular sieve is connected to an inlet of the first section of synthesis gas compressor, a non-permeation gas outlet of the membrane separator is connected to an inlet of an expander, an outlet of the expander is connected to a cold side inlet of a heat exchanger, a cold side outlet of the heat exchanger is connected to a cold side inlet of a heater, and a cold side outlet of the heater is connected to an inlet of the regenerated drying tower.
As a further improvement of the technical proposal of the utility model, the hot side inlet of the heat exchanger is connected to the outlet of the synthetic ammonia system.
As the further improvement of the technical proposal of the utility model, the outlet of the regeneration drying tower is connected to the combustion furnace.
As a further improvement of the technical proposal of the utility model, the hot side inlet of the heat exchanger is connected to the outlet of the first ammonia cooler on the outlet of the synthetic ammonia system.
Hydrogen recovery pressure energy and gaseous comprehensive utilization system compare with prior art, have following beneficial effect:
(1) The utility model cancels the heater at the outlet of the water washing tower, adds the drying tower, dries the gas passing through the water washing tower, ensures that the water-gas concentration in the gas can meet the regeneration requirements of the expansion machine and the molecular sieve, uses the non-permeable gas in the system as the regeneration gas of the drying tower, and does not waste the gas of other systems;
(2) The non-permeable gas of the membrane separator in the utility model is decompressed by the expander to recover the pressure energy of the non-permeable gas;
(3) The utility model exchanges heat between the low-temperature gas expanded by the expander and the gas ammonia of the synthetic ammonia system to recover cold;
(4) The utility model provides a membrane separator's permeate gas uses as the regeneration gas of molecular sieve, and the molecular sieve no longer uses qualified technology gas regeneration, reduces the cyclic compression of regeneration gas at one section synthetic gas compressor to increase the effective work of compressor.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic connection diagram of a conventional ammonia synthesis plant.
Fig. 2 is a schematic connection diagram of the hydrogen recovery pressure energy and gas comprehensive utilization system of the present invention.
In the figure: 1-a first-stage synthesis gas compressor, 2-a double-stage purification system, 3-an operating molecular sieve, 4-a regenerated molecular sieve, 5-a second-stage synthesis gas compressor, 6-a synthesis ammonia system, 7-a water washing tower, 8-a heater, 9-a membrane separator, 10-a pressure reducing valve, 11-an operating drying tower, 12-a regenerated drying tower, 13-an expander and 14-a heat exchanger.
Detailed Description
The technical solutions of the present invention will be described clearly and completely below, and it should be apparent that the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
As shown in fig. 2, the utility model provides a specific embodiment of a hydrogen recovery pressure energy and gas comprehensive utilization system, which comprises a first-stage synthesis gas compressor 1, a double-stage purification system 2, a running molecular sieve 3, a regenerated molecular sieve 4, a second-stage synthesis gas compressor 5, a synthesis ammonia system 6, a water washing tower 7, a heater 8 and a membrane separator 9; the system further comprises a running drying tower 11 and a regenerating drying tower 12, wherein the first-stage synthesis gas compressor 1, the double-methanol purification system 2, the running molecular sieve 3, the second-stage synthesis gas compressor 5, the ammonia synthesis system 6 and the water washing tower 7 are sequentially connected, an inlet of the running drying tower 11 is connected with an outlet of the water washing tower 7, an outlet of the running drying tower 11 is connected with an inlet of a membrane separator 9, a permeating gas outlet of the membrane separator 9 is connected with an inlet of the regenerating molecular sieve 4, an outlet of the regenerating molecular sieve 4 is connected with an inlet of the first-stage synthesis gas compressor 1, a non-permeating gas outlet of the membrane separator 9 is connected with an inlet of an expander 13, an outlet of the expander 13 is connected with a cold-side inlet of a heat exchanger 14, a cold-side outlet of the heat exchanger 14 is connected with a cold-side inlet of a heater 8, and a cold-side outlet of the heater 8 is connected with an inlet of the regenerating drying tower 12.
In this embodiment, the double-methanol purification system 2 and the ammonia synthesis system 6 are of a structure known in the art, wherein the double-methanol purification system 2 comprises a methanol synthesis tower, a methanol cooler, a methanol separator, a methanol water washing tower, a methane synthesis tower, a circulating water cooler, an ammonia cooler and a water separator, and the hydrogen peroxide is used as hydrogen 2 、N 2 The main decarbonizing gas contains a small amount of CO and CO 2 Most of CO and CO in the methanol synthesis tower 2 Synthesizing into methanol gas, passing the methanol-containing gas out of the methanol synthesis tower through a methanol cooler to form methanol liquid, passing the gas-liquid mixture through a methanol separator, separating the methanol liquid from the gas-liquid mixture by the methanol separator, passing the mixed gas separated by the methanol separator through a methanol water washing tower, further washing the methanol gas in the purified gas, conveying the gas out of the methanol water washing tower to the methane synthesis tower, and conveying the residual small amount of CO and CO to the methane synthesis tower 2 Conversion to methaneGas, which meets the requirements of CO and CO in gas entering a synthetic ammonia system 6 2 And the gas discharged from the methane synthesis tower is cooled by circulating water of a circulating water cooler and ammonia of an ammonia cooler according to the trace requirement, part of water vapor in the gas discharged from the methane synthesis tower is condensed into liquid water, and then the liquid water enters a water separator to separate condensed water in the gas so as to reduce the concentration of the gas water vapor entering a molecular sieve system. Wherein the synthetic ammonia system 6 comprises an ammonia synthesis tower, a synthetic waste heat boiler, a gas heat exchanger, a circulating water cooler, a two-stage ammonia cooler and an ammonia separator.
The specific workflow of this embodiment is as follows: the decarbonized gas enters a double-A purification system 2 after being subjected to first-stage compression by a first-stage synthesis gas compressor 1, and most of CO and CO are removed 2 The gas after cooling separation enters a molecular sieve drying system, the molecular sieve drying system comprises two adsorption towers, one adsorption tower is used as an operation molecular sieve 3 to carry out high-pressure low-temperature adsorption, the other adsorption tower is used as a regeneration molecular sieve 4 to carry out decompression heating regeneration, and the two adsorption towers are alternately used to realize continuous purification and adsorption of the gas. Purifying and adsorbing fresh gas H by using a running molecular sieve 3 2 、N 2 The gas ammonia is compressed by a two-stage synthesis gas compressor 5 and is supplemented into an ammonia synthesis system 6, the ammonia synthesis tower is used for synthesizing gas ammonia, the reaction heat of the ammonia synthesis tower is utilized to produce steam as a byproduct in a synthesis waste heat boiler, the gas ammonia is subjected to gas heat exchange, circulating water cooling and condensation by a first ammonia cooler to form a gas-liquid mixture, the gas-liquid mixture is further condensed by a second ammonia cooler, most of the generated gas ammonia is condensed to form liquid ammonia, the liquid ammonia is separated from the gas which is not completely reacted by an ammonia separator, the liquid ammonia is sent into an ammonia storage, and the gas which is not completely reacted enters the ammonia synthesis tower to circulate. Methane is used as inert gas of ammonia synthesis reaction, does not participate in the reaction, but can be accumulated in synthesis recycle gas, part of recycle gas needs to be discharged to control the content of methane in the recycle gas to be stable, the part of discharged gas enters a water washing tower 7 to wash out ammonia gas, and then enters a membrane separator 9 after being dehydrated by an operation drying tower 11 of a drying system, and permeation gas from the membrane separator 9 is used as regeneration gas of a regenerated molecular sieve 4 and sent to the molecular sieve, and returns to the inlet of a section of synthesis gas compressor 1 after being regenerated; the non-permeating gas passes throughThe expander 13 reduces the pressure, and the recovered pressure energy drives a generator to generate power or drives equipment to do work; the decompressed process air has a low temperature and enters a cold side inlet of a heat exchanger 14, the process air is further sent into a heater 8 after being heated by the heat exchanger 14, and the heated non-permeable air is sent into a regeneration drying tower 12 as regeneration air of the regeneration drying tower 12 and then sent to a combustion furnace for combustion.
In this example, the pairs H are arranged in the run molecular sieves 3 and the regenerated molecular sieves 4 2 O and CO 2 The 13X type molecular sieve with stronger adsorption capacity is used as an adsorbent to remove oxide impurities in fresh gas, so that the requirement that oxygen-containing compounds are less than or equal to 1ppm is met.
In this embodiment, the drying system includes two drying towers, one of the drying towers is used as the operation drying tower 11 for adsorption water removal, the other drying tower is used as the regeneration drying tower 12 for heating regeneration, and the two drying towers are used alternately to realize continuous drying of the gas.
In practice, the hot-side inlet of the heat exchanger 14 is connected to the outlet of the ammonia synthesis system 6. Specifically, the hot side inlet of the heat exchanger 14 is connected to the outlet of the first ammonia cooler at the outlet of the ammonia synthesis system 6. The gas ammonia from the first ammonia cooler is condensed into liquid ammonia after passing through the heat exchanger 14, and the liquid ammonia is supplemented to the second ammonia cooler for reducing the work of the ice machine.
As shown in fig. 2, the outlet of the regenerative drying tower 12 is connected to a burner.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention.
Claims (4)
1. A hydrogen recovery pressure energy and gas comprehensive utilization system comprises a first-stage synthesis gas compressor (1), a double-stage purification system (2), an operation molecular sieve (3), a regeneration molecular sieve (4), a second-stage synthesis gas compressor (5), an ammonia synthesis system (6), a water washing tower (7), a heater (8) and a membrane separator (9), and is characterized in that,
the system is characterized by further comprising a running drying tower (11) and a regeneration drying tower (12), wherein the first-stage synthesis gas compressor (1), the double-stage purification system (2), the running molecular sieve (3), the second-stage synthesis gas compressor (5), the ammonia synthesis system (6) and the water washing tower (7) are sequentially connected, an inlet of the running drying tower (11) is connected with an outlet of the water washing tower (7), an outlet of the running drying tower (11) is connected with an inlet of the membrane separator (9), a permeation gas outlet of the membrane separator (9) is connected with an inlet of the regeneration molecular sieve (4), an outlet of the regeneration molecular sieve (4) is connected to an inlet of the first-stage synthesis gas compressor (1), a non-permeation gas outlet of the membrane separator (9) is connected to an inlet of an expander (13), an outlet of the expander (13) is connected to a cold-side inlet of a heat exchanger (14), an outlet of the heat exchanger (14) is connected to a cold-side inlet of a heater (8), and a cold-side outlet of the heater (8) is connected to an inlet of the regeneration drying tower (12).
2. A hydrogen recovery pressure energy and gas combined use system according to claim 1, characterized in that the hot side inlet of the heat exchanger (14) is connected to the outlet of the ammonia synthesis system (6).
3. A hydrogen recovery pressure energy and gas integrated utilization system according to claim 1, characterized in that the outlet of the regenerative drying tower (12) is connected to a combustion furnace.
4. A hydrogen recovery pressure energy and gas combined use system according to claim 2, characterized in that the hot side inlet of the heat exchanger (14) is connected to the outlet of the first ammonia cooler at the outlet of the ammonia synthesis system (6).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202221953229.3U CN217868148U (en) | 2022-07-27 | 2022-07-27 | Hydrogen recovery pressure energy and gas comprehensive utilization system |
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| CN202221953229.3U CN217868148U (en) | 2022-07-27 | 2022-07-27 | Hydrogen recovery pressure energy and gas comprehensive utilization system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116081644A (en) * | 2023-02-14 | 2023-05-09 | 中国成达工程有限公司 | A flexible synthetic ammonia preparation system and process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116081644A (en) * | 2023-02-14 | 2023-05-09 | 中国成达工程有限公司 | A flexible synthetic ammonia preparation system and process |
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