CN108826830A - A kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas - Google Patents
A kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas Download PDFInfo
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- CN108826830A CN108826830A CN201810764839.0A CN201810764839A CN108826830A CN 108826830 A CN108826830 A CN 108826830A CN 201810764839 A CN201810764839 A CN 201810764839A CN 108826830 A CN108826830 A CN 108826830A
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- cold energy
- energy recovery
- recovery unit
- rectifying column
- unit
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- 238000011084 recovery Methods 0.000 title claims abstract description 87
- 239000007789 gas Substances 0.000 title claims abstract description 42
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 25
- 239000003507 refrigerant Substances 0.000 claims abstract description 48
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 14
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 10
- 238000002309 gasification Methods 0.000 claims abstract description 7
- 238000004064 recycling Methods 0.000 claims description 12
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 238000003786 synthesis reaction Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 abstract description 18
- 229910021529 ammonia Inorganic materials 0.000 abstract description 4
- 238000004821 distillation Methods 0.000 abstract description 4
- 239000002826 coolant Substances 0.000 description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 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
- 238000005915 ammonolysis reaction Methods 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
- 238000005516 engineering process Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000012946 outsourcing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 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
- 239000004615 ingredient Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002994 raw material 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
-
- 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)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
- Industrial Gases (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention discloses a kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas, liquefied natural gas in liquified natural gas tank enters in the first cold energy recovery unit exchanged heat after it is outer defeated；Refrigerant as the cold source of de- C1 rectifying column and de- C2 rectifying column and providing respectively enter after cold energy second and third cold energy recovery unit form heat exchange cycle with the first cold energy recovery unit again；The rich H2 stream stock of de- the top of the distillation column C1 recycles cooling capacity, rich H of the coke-stove gas through exchanging heat by the 4th cold energy recovery unit2Flow preparing ammonia after stock purifies；The charging that coke-stove gas enters in second and third and four cold energy recovery units after pre-cooling as de- C2 rectifying column simultaneously enters in rectifying column in the middle part of tower isolates C2 component.The present invention can efficiently be separated the high added value component in coke-stove gas using the cold energy that liquefied natural gas is generated in gasification one by one, obtain the higher high value added product C of purity2H4With rich H2Gas is simultaneously used.
Description
Technical field
The present invention relates to coke-stove gas utilization technology fields, and in particular to a kind of to utilize cold energy focusing of being warm of liquefying
The system that producer gas is recycled.
Background technique
Coke-stove gas is the mixed gas that generates in coking industry production, constituent ratio, with coking technology with
The difference of working condition and there are difference.Contain H in coke-stove gas after the techniques such as water removal, sulphur2、C2H4Etc. high added values
Component, recovery difficult is high, and at present there is no good recoverying and utilizing method, some producers then select to burn it as conventional fuel
Fall, serious waste of resources.
Liquefied natural gas can provide the low temperature position cooling capacity of a large amount of cold energy and high-quality in gasification, but above-mentioned low temperature
Position cooling capacity is not also reasonably utilized, and the valuable energy has equally been lost.
Summary of the invention
In view of this, the present invention provides a kind of intermediate feed coke-stove gas using cold energy of liquefied natural gas to recycle system
System can efficiently be divided the high added value component in coke-stove gas using the cold energy that liquefied natural gas is generated in gasification one by one
From obtaining the higher high value added product C of purity2H4With rich H2Gas is simultaneously used.
A kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas, which includes liquefied natural gas
Tank, the first cold energy recovery unit, the second cold energy recovery unit, third cold energy recovery unit, the 4th cold energy recovery unit, de- C1 essence
Evaporate tower, de- C2 rectifying column, clean unit, psa unit and synthesis ammonia unit；
Wherein, the first cold energy recovery unit, the second cold energy recovery unit, third cold energy recovery unit and the recycling of the 4th cold energy
The structure of unit is identical, all has refrigerant inlet and outlet and medium inlet and outlet；
The liquified natural gas tank is connected to the medium entrance of the first cold energy recovery unit, passes through after liquefied natural gas heat exchange gasification
Media outlet is exported outward to user；The refrigerant inlet of the refrigerant exit of 4th cold energy recovery unit and the first cold energy recovery unit
The refrigerant exit of connection, the first cold energy recovery unit is connected to the tower top of de- C1 rectifying column and de- C2 rectifying column simultaneously；De- C1 essence
The refrigerant exit and product exit that evaporate tower side are respectively communicated with the refrigerant of the 4th cold energy recovery unit and the second cold energy recovery unit
Entrance, the refrigerant exit connection psa unit and synthesis ammonia unit of the second cold energy recovery unit；The refrigerant of de- C2 rectifying column
The refrigerant inlet of outlet connection third cold energy recovery unit, the refrigerant exit of third cold energy recovery unit connect the recycling of the first cold energy
The refrigerant inlet of unit；
Coke-stove gas outside the entrance access of the clean unit, the outlet of clean unit is separately connected after being divided into three tunnels
The medium inlet of second cold energy recovery unit, third cold energy recovery unit and the 4th cold energy recovery unit, above three cold energy return
The media outlet of receipts unit connects the middle part charging of de- C2 rectifying column after converging, take off the de- C1 rectifying column of tower top connection of C2 rectifying column
Tower top.
Further, the bottom of the de- C1 rectifying column and de- C2 rectifying column has tower bottom product separation outlet.
Further, the refrigerant inlet of the second cold energy recovery unit and the refrigerant of outlet access are in de- C1 rectifying column
The rich H2 stream stock isolated.
Beneficial effect：
The present invention carries out the high added value ingredient in coke-stove gas by the cold energy that liquefied natural gas is provided in gasification
It effectively recycles and utilizes, the high-quality cold energy and coke-stove gas resource of liquefied natural gas offer are provided, economy is realized
It maximizes to benefit, while also complying with the general requirement of national energy conservation and emission reduction.
Detailed description of the invention
Fig. 1 is system theory of constitution schematic diagram of the invention.
Specific embodiment
The present invention will now be described in detail with reference to the accompanying drawings and examples.
As shown in Fig. 1, the present invention provides a kind of intermediate feed coke-stove gas recycling using cold energy of liquefied natural gas
System, the system include liquified natural gas tank, the first cold energy recovery unit, the second cold energy recovery unit, third cold energy recycling list
Member, the 4th cold energy recovery unit, de- C1 rectifying column, de- C2 rectifying column, clean unit, psa unit and synthesis ammonia unit；
The function of de- C1 rectifying column is to separate the Hydrocarbon Organic containing a carbon atom in coke-stove gas, such as first
Alkane；De- C2 rectifying column is will to contain that there are two the Hydrocarbon Organics of carbon atom to separate, such as ethane and ethylene.
Wherein, the first cold energy recovery unit, the second cold energy recovery unit, third cold energy recovery unit and the recycling of the 4th cold energy
The structure of unit is identical, all has refrigerant inlet and outlet and medium inlet and outlet；The bottom of de- C1 rectifying column and de- C2 rectifying column has
Tower bottom product separation outlet.
Liquified natural gas tank is connected to the medium entrance of the first cold energy recovery unit, through medium after liquefied natural gas heat exchange gasification
Outlet is exported to user outward；The refrigerant inlet of the refrigerant exit of 4th cold energy recovery unit and the first cold energy recovery unit connects
Logical, the refrigerant exit of the first cold energy recovery unit is connected to the tower top of de- C1 rectifying column and de- C2 rectifying column simultaneously；De- C1 rectifying
The refrigerant exit and product exit of tower side are respectively communicated with the 4th cold energy recovery unit and the refrigerant of the second cold energy recovery unit enters
Mouthful, the refrigerant exit connection psa unit and synthesis ammonia unit of the second cold energy recovery unit, the second cold energy recovery unit
Refrigerant inlet and the refrigerant of outlet access are the rich H2 stream stocks isolated in de- C1 rectifying column；The refrigerant exit of de- C2 rectifying column connects
The refrigerant inlet of third cold energy recovery unit is connect, the refrigerant exit of third cold energy recovery unit connects the first cold energy recovery unit
Refrigerant inlet；
Coke-stove gas outside the entrance access of clean unit, the outlet of clean unit is separately connected second after being divided into three tunnels
The medium inlet of cold energy recovery unit, third cold energy recovery unit and the 4th cold energy recovery unit, the recycling of above three cold energy are single
The media outlet of member connects the middle part charging of de- C2 rectifying column after converging, the tower top for taking off C2 rectifying column is connected to the tower of de- C1 rectifying column
Top.
Working principle：Liquefied natural gas (LNG) is exported from storage tank, and the liquefied natural gas 1 for being pressurized to specified pressure enters the
Cold energy is passed to gaseous coolant 7, gaseous state by one cold energy recovery unit, the liquefied natural gas gasifying in the first cold energy recovery unit
Refrigerant 7 becomes liquid refrigerants 3 and liquid refrigerants 4, storage of cold from gaseous state.It is outer defeated after pressurizeing with the natural gas 2 after refrigerant heat exchange,
It is used for natural gas user.
Cold source of the liquid refrigerants 3 as de- the top of the distillation column C1, becomes gaseous state after providing demand cooling capacity for de- C1 rectifying column,
Gaseous coolant 6 further recycles the cooling capacity in gaseous coolant into the 4th cold energy recovery unit, to be pre-chilled by purified treatment
Coke-stove gas 21 afterwards.Gaseous coolant 14 after the 4th cold energy recovery unit recycles cooling capacity is mixed with gaseous coolant 13；Liquid
Cold source of the state refrigerant 4 as de- the top of the distillation column C2, becomes gaseous state, gaseous coolant 12 after providing demand cooling capacity for de- C2 rectifying column
The cooling capacity in gaseous coolant is further recycled into third cold energy recovery unit, the coke-oven coal after purified treatment is pre-chilled
Gas 17, the gaseous coolant 13 after third cold energy recovery unit recycles cooling capacity are mixed into gaseous coolant 14, mixed gas
State refrigerant 7 continues to store the cold energy in LNG back to the first cold energy recovery unit.
The charging of de- C1 rectifying column carrys out the overhead fraction 8 of autospasy C2 rectifying column, and C1 liquid phase is isolated at de- C1 rectifying tower bottom
Component 5, the fraction that tower top is isolated are mainly H2, in addition also containing components such as a small amount of N2, Ar, CO.De- the top of the distillation column C1
Rich H2 stream stock 9 recycles cooling capacity by the second cold energy recovery unit, cooling to pass through purified coke-stove gas 20, then by changing
The rich H2 stream stock 19 of heat further purifies H2 into pressure swing adsorption system.High-purity hydrogen 25 after purification and outsourcing nitrogen 26 into
Enter Ammonia Production device preparing ammonia 27.
By de- S, de- H2O, treated that coke-stove gas 24 enters purification system emergence work 23.Purified coke-stove gas
22 points are pre-chilled for three parts.Wherein purified coke-stove gas 20 enters in the second cold energy recovery unit, de- by recycling
The rich H2 of C1 column overhead flows the cooling capacity in stock 9 and is cooled；Purified coke-stove gas 17 enters in third cold energy recovery unit,
It is cooled by the cooling capacity in recycling gaseous coolant 12, the gaseous coolant of cooling capacity is further recycled by third cold energy recovery unit
13 mix with other gaseous coolants 14；Purified coke-stove gas 21 enters in the 4th cold energy recovery unit, by recycling gaseous state
Cooling capacity in refrigerant 6 and be cooled, the gaseous coolant 14 and gaseous coolant of cooling capacity are further recycled by the 4th cold energy recovery unit
13 mixing, mixed gaseous coolant 7 return in the first cold energy recovery unit.
Cooled coke-stove gas 18, coke-stove gas 16 and coke-stove gas 15 mixes, mixed cooling coke-stove gas 10
Charging as de- C2 rectifying column enters in de- C2 rectifying column from tower medium position.Isolate C2 component in de- C2 rectifying tower bottom
The light component 8 of 11, mainly ethylene component, tower top separation enters abjection C1 rectifying column as raw material.
By taking the coke-stove gas of certain factory 50000Nm3/h utilizes as an example：The group of coke-stove gas becomes H257.00%, N2
5.00%, CO 7.00%, O20.50%, CH425.00%, CO23.00%, C2H42.50%.The technique can produce 1.1 in year
Ten thousand tons of C2H4Product and 70,000 tons of LNG (CH4) products, in addition, richness H2Gas by pressure swing adsorption system into becoming high-purity hydrogen, it is high
Pure hydrogen and outsourcing (or product in factory) nitrogen enter Ammonia Production device and produce ammonolysis product.It can be achieved 100,000 tons/year
Ammonolysis product production is synthesized, there is great economic benefit.
In conclusion the above is merely preferred embodiments of the present invention, being not intended to limit the scope of the present invention.
All within the spirits and principles of the present invention, any modification, equivalent replacement, improvement and so on should be included in of the invention
Within protection scope.
Claims (3)
1. a kind of intermediate feed coke-stove gas recovery system using cold energy of liquefied natural gas, which is characterized in that the system includes
Liquified natural gas tank, the first cold energy recovery unit, the second cold energy recovery unit, third cold energy recovery unit, the recycling of the 4th cold energy
Unit, de- C1 rectifying column, de- C2 rectifying column, clean unit, psa unit and synthesis ammonia unit；
Wherein, the first cold energy recovery unit, the second cold energy recovery unit, third cold energy recovery unit and the 4th cold energy recovery unit
Structure it is identical, all have refrigerant inlet and outlet and medium inlet and outlet；
The liquified natural gas tank is connected to the medium entrance of the first cold energy recovery unit, through medium after liquefied natural gas heat exchange gasification
Outlet is exported to user outward；The refrigerant inlet of the refrigerant exit of 4th cold energy recovery unit and the first cold energy recovery unit connects
Logical, the refrigerant exit of the first cold energy recovery unit is connected to the tower top of de- C1 rectifying column and de- C2 rectifying column simultaneously；De- C1 rectifying
The refrigerant exit and product exit of tower side are respectively communicated with the 4th cold energy recovery unit and the refrigerant of the second cold energy recovery unit enters
Mouthful, the refrigerant exit connection psa unit and synthesis ammonia unit of the second cold energy recovery unit；The refrigerant of de- C2 rectifying column goes out
The refrigerant inlet of mouth connection third cold energy recovery unit, it is single that the refrigerant exit of third cold energy recovery unit connects the recycling of the first cold energy
The refrigerant inlet of member；
Coke-stove gas outside the entrance access of the clean unit, the outlet of clean unit is separately connected second after being divided into three tunnels
The medium inlet of cold energy recovery unit, third cold energy recovery unit and the 4th cold energy recovery unit, the recycling of above three cold energy are single
The media outlet of member connects the middle part charging of de- C2 rectifying column after converging, the tower top for taking off C2 rectifying column is connected to the tower of de- C1 rectifying column
Top.
2. utilizing the intermediate feed coke-stove gas recovery system of cold energy of liquefied natural gas as described in claim 1, feature exists
In the bottom of the de- C1 rectifying column and de- C2 rectifying column has tower bottom product separation outlet.
3. utilizing the intermediate feed coke-stove gas recovery system of cold energy of liquefied natural gas, feature as claimed in claim 1 or 2
It is, the refrigerant inlet of the second cold energy recovery unit and the refrigerant of outlet access are the rich H2 isolated in de- C1 rectifying column
Flow stock.
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 |
Applications Claiming Priority (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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| Publication Number | Publication Date |
|---|---|
| CN108826830A true CN108826830A (en) | 2018-11-16 |
| CN108826830B CN108826830B (en) | 2024-01-09 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110387274A (en) * | 2019-07-20 | 2019-10-29 | 中科瑞奥能源科技股份有限公司 | It is pyrolyzed the equipment and method of coal gas LNG coproduction LPG |
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