CN108826830B - Intermediate feeding coke oven gas recovery system utilizing liquefied natural gas cold energy - Google Patents
Intermediate feeding coke oven gas recovery system utilizing liquefied natural gas cold energy Download PDFInfo
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- CN108826830B CN108826830B CN201810764839.0A CN201810764839A CN108826830B CN 108826830 B CN108826830 B CN 108826830B CN 201810764839 A CN201810764839 A CN 201810764839A CN 108826830 B CN108826830 B CN 108826830B
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- cold energy
- energy recovery
- recovery unit
- rectifying tower
- refrigerant
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- 238000011084 recovery Methods 0.000 title claims abstract description 103
- 239000007789 gas Substances 0.000 title claims abstract description 52
- 239000000571 coke Substances 0.000 title claims abstract description 36
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 30
- 239000003507 refrigerant Substances 0.000 claims abstract description 61
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000002309 gasification Methods 0.000 claims abstract description 7
- 238000001179 sorption measurement Methods 0.000 claims description 8
- 238000000746 purification Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 abstract description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- AFYPFACVUDMOHA-UHFFFAOYSA-N chlorotrifluoromethane Chemical compound FC(F)(F)Cl AFYPFACVUDMOHA-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- TXEYQDLBPFQVAA-UHFFFAOYSA-N tetrafluoromethane Chemical compound FC(F)(F)F TXEYQDLBPFQVAA-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- PXBRQCKWGAHEHS-UHFFFAOYSA-N dichlorodifluoromethane Chemical compound FC(F)(Cl)Cl PXBRQCKWGAHEHS-UHFFFAOYSA-N 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B27/00—Arrangements for withdrawal of the distillation gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The invention discloses a middle feeding coke oven gas recovery system utilizing liquefied natural gas cold energy, wherein the liquefied natural gas in a liquefied natural gas tank enters a first cold energy recovery unit for heat exchange and then is conveyed outwards; the refrigerant is used as a cold source of the C1 removal rectifying tower and the C2 removal rectifying tower, and after cold energy is provided, the refrigerant enters the second cold energy recovery unit and the third cold energy recovery unit respectively, and then forms heat exchange circulation with the first cold energy recovery unit; the H2-enriched stream at the top of the C1-removal rectifying tower is used for recovering cold energy through a fourth cold energy recovery unit, and the coke oven gas is subjected to heat exchange to be H-enriched 2 Purifying the flow to prepare ammonia; the coke oven gas enters the second, third and fourth cold energy recovery units simultaneously for precooling and then enters the rectifying tower from the middle part of the tower as the feed of the C2 rectifying tower to separate out C2 components. The invention can effectively utilize the cold energy generated by the gasification of the liquefied natural gas to separate the high added value components in the coke oven gas one by one, thus obtaining the high added value product C with higher purity 2 H 4 And is rich in H 2 The gas is used.
Description
Technical Field
The invention relates to the technical field of coke oven gas recycling, in particular to a system for recycling coke oven gas by utilizing hot and cold energy of liquefied weather.
Background
Coke oven gas is a mixed gas produced in coking industry, and the ratio of the constituent components varies with the coking technique and the production conditions. The coke oven gas after the processes of water removal, sulfur and the like contains H 2 、C 2 H 4 The components with equal high added value have high recycling difficulty, no good recycling method exists at present, and some manufacturers select the components to be used as common fuel to be burnt, so that the resource waste is serious.
The liquefied natural gas can provide a large amount of cold energy and high-quality low-temperature cold energy during gasification, but the low-temperature cold energy is not reasonably utilized, and precious energy is also lost.
Disclosure of Invention
In view of the above, the invention provides a middle-feed coke oven gas recovery system utilizing liquefied natural gas cold energy, which can efficiently utilize cold energy generated by gasification of liquefied natural gas to separate high-added-value components in coke oven gas one by one, thus obtaining a high-added-value product C with higher purity 2 H 4 And is rich in H 2 The gas is used.
The system comprises a liquefied natural gas tank, a first cold energy recovery unit, a second cold energy recovery unit, a third cold energy recovery unit, a fourth cold energy recovery unit, a C1 removal rectifying tower, a C2 removal rectifying tower, a purifying unit, a pressure swing adsorption unit and a synthetic ammonia unit;
the first cold energy recovery unit, the second cold energy recovery unit, the third cold energy recovery unit and the fourth cold energy recovery unit have the same structure and are provided with a refrigerant inlet and a medium outlet;
the liquefied natural gas tank is communicated with a medium inlet of the first cold energy recovery unit, and liquefied natural gas is subjected to heat exchange gasification and then is output to a user through a medium outlet; the refrigerant outlet of the fourth cold energy recovery unit is communicated with the refrigerant inlet of the first cold energy recovery unit, and the refrigerant outlet of the first cold energy recovery unit is simultaneously communicated with the tops of the C1 removal rectifying tower and the C2 removal rectifying tower; the refrigerant outlet and the product outlet on the side surface of the C1 removal rectifying tower are respectively communicated with the refrigerant inlets of the fourth cold energy recovery unit and the second cold energy recovery unit, and the refrigerant outlet of the second cold energy recovery unit is communicated with the pressure swing adsorption unit and the synthetic ammonia unit; the refrigerant outlet of the C2 removal rectifying tower is connected with the refrigerant inlet of the third cold energy recovery unit, and the refrigerant outlet of the third cold energy recovery unit is connected with the refrigerant inlet of the first cold energy recovery unit;
the inlet of the purifying unit is connected with external coke oven gas, the outlet of the purifying unit is divided into three paths and then is respectively connected with medium inlets of the second cold energy recovery unit, the third cold energy recovery unit and the fourth cold energy recovery unit, medium outlets of the three cold energy recovery units are converged and then are connected with middle feeding of the C2 stripping rectifying tower, and the top of the C2 stripping rectifying tower is communicated with the top of the C1 stripping rectifying tower.
Further, bottoms of the C1-removing rectifying tower and the C2-removing rectifying tower are provided with bottom product separation outlets.
Further, the refrigerant introduced from the refrigerant inlet and the refrigerant introduced from the refrigerant outlet of the second cold energy recovery unit are H2-rich streams separated from the C1-removal rectifying tower.
The beneficial effects are that:
the invention effectively recovers and utilizes the high added value components in the coke oven gas through the cold energy provided by the liquefied natural gas in gasification, fully utilizes the high-quality cold energy provided by the liquefied natural gas and the coke oven gas resource, realizes the maximization of economic benefit, and meets the overall requirements of national energy conservation and emission reduction.
Drawings
FIG. 1 is a schematic diagram of the system composition principle of the present invention.
Detailed Description
The invention will now be described in detail by way of example with reference to the accompanying drawings.
As shown in fig. 1, the invention provides a middle-feed coke oven gas recovery system utilizing liquefied natural gas cold energy, which comprises a liquefied natural gas tank, a first cold energy recovery unit, a second cold energy recovery unit, a third cold energy recovery unit, a fourth cold energy recovery unit, a C1 removal rectifying tower, a C2 removal rectifying tower, a purification unit, a pressure swing adsorption unit and a synthetic ammonia unit;
the C1-removing rectifying tower has the function of separating hydrocarbon organic matters containing one carbon atom from coke oven gas, such as methane; the C2-removing rectifying tower separates hydrocarbon organic matter containing two carbon atoms, such as ethane and ethylene.
The first cold energy recovery unit, the second cold energy recovery unit, the third cold energy recovery unit and the fourth cold energy recovery unit have the same structure and are provided with a refrigerant inlet and a medium outlet; the bottoms of the C1-removing rectifying tower and the C2-removing rectifying tower are provided with bottom product separation outlets.
The liquefied natural gas tank is communicated with a medium inlet of the first cold energy recovery unit, and the liquefied natural gas is subjected to heat exchange gasification and then is outwards output to a user through a medium outlet; the refrigerant outlet of the fourth cold energy recovery unit is communicated with the refrigerant inlet of the first cold energy recovery unit, and the refrigerant outlet of the first cold energy recovery unit is simultaneously communicated with the tops of the C1 removal rectifying tower and the C2 removal rectifying tower; the refrigerant outlet and the product outlet on the side surface of the C1 removal rectifying tower are respectively communicated with the refrigerant inlets of the fourth cold energy recovery unit and the second cold energy recovery unit, the refrigerant outlet of the second cold energy recovery unit is communicated with the pressure swing adsorption unit and the synthetic ammonia unit, and the refrigerant inlet and the refrigerant outlet of the second cold energy recovery unit are connected with the refrigerant inlet and the refrigerant outlet of the second cold energy recovery unit to form an H2-enriched stream separated from the C1 removal rectifying tower; the refrigerant outlet of the C2 removal rectifying tower is connected with the refrigerant inlet of the third cold energy recovery unit, and the refrigerant outlet of the third cold energy recovery unit is connected with the refrigerant inlet of the first cold energy recovery unit;
the inlet of the purifying unit is connected with external coke oven gas, the outlet of the purifying unit is divided into three paths and then is respectively connected with medium inlets of the second cold energy recovery unit, the third cold energy recovery unit and the fourth cold energy recovery unit, medium outlets of the three cold energy recovery units are converged and then are connected with middle feeding of the C2 stripping rectifying tower, and the top of the C2 stripping rectifying tower is communicated with the top of the C1 stripping rectifying tower.
Working principle: liquefied Natural Gas (LNG) is output from a storage tank, the liquefied natural gas 1 pressurized to a specific pressure enters a first cold energy recovery unit, the liquefied natural gas is gasified in the first cold energy recovery unit, cold energy is transmitted to a gaseous refrigerant 7, the gaseous refrigerant 7 is changed into a liquid refrigerant 3 and a liquid refrigerant 4 from the gas state, and the cold energy is stored. And the natural gas 2 subjected to heat exchange with the refrigerant is pressurized and then is output for a natural gas user to use.
The liquid refrigerant 3 is used as a cold source at the top of the C1 removal rectifying tower, provides required cold energy for the C1 removal rectifying tower, and then turns into a gas state, and the gas refrigerant 6 enters a fourth cold energy recovery unit to further recover the cold energy in the gas refrigerant so as to precool the coke oven gas 21 after the purification treatment. The gaseous refrigerant 14 after cold energy recovery through the fourth cold energy recovery unit is mixed with the gaseous refrigerant 13; the liquid refrigerant 4 is used as a cold source at the top of the C2 removal rectifying tower, the cold energy required by the C2 removal rectifying tower is provided, the liquid refrigerant is changed into a gas state, the gas refrigerant 12 enters a third cold energy recovery unit to further recover the cold energy in the gas refrigerant, the gas refrigerant is used for precooling the coke oven gas 17 after the purification treatment, the gas refrigerant 13 after the cold energy recovery by the third cold energy recovery unit is mixed with the gas refrigerant 14 to form the mixed gas refrigerant 7, and the mixed gas refrigerant returns to the first cold energy recovery unit to continuously store the cold energy in LNG.
The feeding of the C1-removing rectifying tower is from the top fraction 8 of the C2-removing rectifying tower, the C1 liquid phase component 5 is separated from the bottom of the C1-removing rectifying tower, the separated fraction at the top of the tower is mainly H2, and the separated fraction also contains a small amount of N2, ar, CO and other components. The H2-enriched stream 9 at the top of the C1-removal rectifying tower is subjected to cold energy recovery through a second cold energy recovery unit, the purified coke oven gas 20 is cooled, and then the H2-enriched stream 19 subjected to heat exchange enters a pressure swing adsorption system to further purify H2. Purified high-purity hydrogen 25 and outsourced nitrogen 26 enter a synthetic ammonia production device to prepare ammonia 27.
The coke oven gas 24 after S and H2O removal treatment enters a purification system to remove CO223. The purified coke oven gas 22 is divided into three parts for precooling. Wherein the purified coke oven gas 20 enters a second cold energy recovery unit and is cooled by recovering cold energy in an H2-rich stream 9 at the top of the C1 removal tower; the purified coke oven gas 17 enters a third cold energy recovery unit, is cooled by recovering cold energy in the gaseous refrigerant 12, and the gaseous refrigerant 13 with the cold energy recovered by the third cold energy recovery unit is mixed with other gaseous refrigerants 14; the purified coke oven gas 21 enters the fourth cold energy recovery unit, is cooled by recovering the cold energy in the gaseous refrigerant 6, the gaseous refrigerant 14 further recovering the cold energy by the fourth cold energy recovery unit is mixed with the gaseous refrigerant 13, and the mixed gaseous refrigerant 7 is returned to the first cold energy recovery unit.
The cooled coke oven gas 18, the coke oven gas 16 and the coke oven gas 15 are mixed, and the mixed cooled coke oven gas 10 is taken as a feed material of the C2-removal rectifying tower to enter the C2-removal rectifying tower from the middle position of the tower. The C2 component 11 is separated from the bottom of the C2-removing rectifying tower, mainly ethylene component, and the light component 8 separated from the top of the tower is taken as raw material to enter the C1-removing rectifying tower.
Taking the coke oven gas utilization of 50000Nm3/h of a certain factory as an example: the coke oven gas has the composition of H 2 57.00％、N 2 5.00％、CO 7.00％、O 2 0.50％、CH 4 25.00％、CO 2 3.00％、C 2 H 4 2.50%. The process can produce 1.1 ten thousand tons of C in a year 2 H 4 Product and 7 ten thousand tons of LNG (CH 4) product, and furthermore, is H-rich 2 The gas is changed into high-purity hydrogen through a pressure swing adsorption system, and the high-purity hydrogen and outsourcing (or product in the factory) nitrogen enter a synthetic ammonia production device to produce ammonia products. Can realize the production of 10 ten thousand tons/year of synthetic ammonia products and has great economic benefit.
In summary, the above embodiments are only preferred embodiments of the present invention, and are not intended to limit the scope of the present invention. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (3)
1. The middle-feeding coke oven gas recovery system utilizing the cold energy of the liquefied natural gas is characterized by comprising a liquefied natural gas tank, a first cold energy recovery unit, a second cold energy recovery unit, a third cold energy recovery unit, a fourth cold energy recovery unit, a C1 removal rectifying tower, a C2 removal rectifying tower, a purification unit, a pressure swing adsorption unit and a synthetic ammonia unit;
the first cold energy recovery unit, the second cold energy recovery unit, the third cold energy recovery unit and the fourth cold energy recovery unit have the same structure and are provided with a refrigerant inlet and a medium outlet;
the liquefied natural gas tank is communicated with a medium inlet of the first cold energy recovery unit, and liquefied natural gas is subjected to heat exchange gasification and then is output to a user through a medium outlet; the refrigerant outlet of the fourth cold energy recovery unit is communicated with the refrigerant inlet of the first cold energy recovery unit, and the refrigerant outlet of the first cold energy recovery unit is simultaneously communicated with the tops of the C1 removal rectifying tower and the C2 removal rectifying tower; the refrigerant outlet and the product outlet on the side surface of the C1 removal rectifying tower are respectively communicated with the refrigerant inlets of the fourth cold energy recovery unit and the second cold energy recovery unit, and the refrigerant outlet of the second cold energy recovery unit is communicated with the pressure swing adsorption unit and the synthetic ammonia unit; the refrigerant outlet of the C2 removal rectifying tower is connected with the refrigerant inlet of the third cold energy recovery unit, and the refrigerant outlet of the third cold energy recovery unit is connected with the refrigerant inlet of the first cold energy recovery unit;
the inlet of the purifying unit is connected with external coke oven gas, the outlet of the purifying unit is divided into three paths and then is respectively connected with medium inlets of the second cold energy recovery unit, the third cold energy recovery unit and the fourth cold energy recovery unit, medium outlets of the second cold energy recovery unit, the third cold energy recovery unit and the fourth cold energy recovery unit are converged and then are connected with middle feeding of the C2 stripping rectifying tower, and the top of the C2 stripping rectifying tower is communicated with the top of the C1 stripping rectifying tower.
2. The intermediate feed coke oven gas recovery system utilizing cold energy of liquefied natural gas as recited in claim 1, wherein bottoms of said de-C1 rectifying column and de-C2 rectifying column have bottoms separation outlets.
3. The intermediate feed coke oven gas recovery system utilizing cold energy of liquefied natural gas as claimed in claim 1 or 2, wherein the refrigerant of the second cold energy recovery unit is an H2-rich stream separated in a C1-stripping rectifying column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810764839.0A CN108826830B (en) | 2018-07-12 | 2018-07-12 | Intermediate feeding coke oven gas recovery system utilizing liquefied natural gas cold energy |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201810764839.0A CN108826830B (en) | 2018-07-12 | 2018-07-12 | Intermediate feeding coke oven gas recovery system utilizing liquefied natural gas cold energy |
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| CN108826830A CN108826830A (en) | 2018-11-16 |
| CN108826830B true CN108826830B (en) | 2024-01-09 |
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| CN110387274B (en) * | 2019-07-20 | 2024-08-02 | 中科瑞奥能源科技股份有限公司 | Equipment and method for preparing LNG and coproducing LPG by pyrolyzing coal gas |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54103797A (en) * | 1978-02-03 | 1979-08-15 | Sumitomo Heavy Ind Ltd | H2 separation and purification from h2 containing gas |
| CN101463281A (en) * | 2007-12-17 | 2009-06-24 | 中国科学院理化技术研究所 | Separation process and equipment for preparing liquefied natural gas from coke oven gas |
| CN202116524U (en) * | 2011-07-13 | 2012-01-18 | 上海国际化建工程咨询公司 | Device for producing liquefied natural gas by coke oven gas through low-temperature rectification |
| CN102435044A (en) * | 2011-12-13 | 2012-05-02 | 杭州中泰深冷技术股份有限公司 | Cryogenic separating system for preparing liquefied natural gas with oven gas |
| CN102519222A (en) * | 2011-12-13 | 2012-06-27 | 杭州中泰深冷技术股份有限公司 | Cryogenic separation method for preparing liquefied natural gas from coke-oven gas |
| CN102654348A (en) * | 2012-05-22 | 2012-09-05 | 中国海洋石油总公司 | Method for producing liquefied natural gas by using coke oven gas |
| CN103697659A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of high methane gas |
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| JP2016090138A (en) * | 2014-11-05 | 2016-05-23 | エア・ウォーター株式会社 | Liquefaction natural gas manufacturing device and liquefaction natural gas manufacturing method |
| CN108240733A (en) * | 2018-01-24 | 2018-07-03 | 北京拓首能源科技股份有限公司 | A kind of air-seperation system using cold energy of liquefied natural gas |
| CN108266965A (en) * | 2018-01-24 | 2018-07-10 | 北京拓首能源科技股份有限公司 | A kind of oxygen nitrogen piece-rate system using cold energy of liquefied natural gas |
| CN208635425U (en) * | 2018-07-12 | 2019-03-22 | 北京拓首能源科技股份有限公司 | A kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas |
-
2018
- 2018-07-12 CN CN201810764839.0A patent/CN108826830B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54103797A (en) * | 1978-02-03 | 1979-08-15 | Sumitomo Heavy Ind Ltd | H2 separation and purification from h2 containing gas |
| CN101463281A (en) * | 2007-12-17 | 2009-06-24 | 中国科学院理化技术研究所 | Separation process and equipment for preparing liquefied natural gas from coke oven gas |
| CN202116524U (en) * | 2011-07-13 | 2012-01-18 | 上海国际化建工程咨询公司 | Device for producing liquefied natural gas by coke oven gas through low-temperature rectification |
| CN102435044A (en) * | 2011-12-13 | 2012-05-02 | 杭州中泰深冷技术股份有限公司 | Cryogenic separating system for preparing liquefied natural gas with oven gas |
| CN102519222A (en) * | 2011-12-13 | 2012-06-27 | 杭州中泰深冷技术股份有限公司 | Cryogenic separation method for preparing liquefied natural gas from coke-oven gas |
| CN102654348A (en) * | 2012-05-22 | 2012-09-05 | 中国海洋石油总公司 | Method for producing liquefied natural gas by using coke oven gas |
| CN103697659A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of high methane gas |
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| JP2016090138A (en) * | 2014-11-05 | 2016-05-23 | エア・ウォーター株式会社 | Liquefaction natural gas manufacturing device and liquefaction natural gas manufacturing method |
| CN108240733A (en) * | 2018-01-24 | 2018-07-03 | 北京拓首能源科技股份有限公司 | A kind of air-seperation system using cold energy of liquefied natural gas |
| CN108266965A (en) * | 2018-01-24 | 2018-07-10 | 北京拓首能源科技股份有限公司 | A kind of oxygen nitrogen piece-rate system using cold energy of liquefied natural gas |
| CN208635425U (en) * | 2018-07-12 | 2019-03-22 | 北京拓首能源科技股份有限公司 | A kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas |
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