CN207751220U - A kind of mixed alkanes reaction product swell refrigeration piece-rate system - Google Patents
A kind of mixed alkanes reaction product swell refrigeration piece-rate system Download PDFInfo
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- CN207751220U CN207751220U CN201820060795.9U CN201820060795U CN207751220U CN 207751220 U CN207751220 U CN 207751220U CN 201820060795 U CN201820060795 U CN 201820060795U CN 207751220 U CN207751220 U CN 207751220U
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- heat exchanger
- reaction product
- throttle valve
- tributary
- knockout drum
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- 239000007795 chemical reaction product Substances 0.000 title claims abstract description 60
- 238000005057 refrigeration Methods 0.000 title claims abstract description 22
- 150000001335 aliphatic alkanes Chemical class 0.000 title claims abstract description 17
- 239000000047 product Substances 0.000 claims abstract description 54
- 239000012530 fluid Substances 0.000 claims abstract description 44
- 239000012071 phase Substances 0.000 claims abstract description 23
- 238000005191 phase separation Methods 0.000 claims abstract description 23
- 239000007791 liquid phase Substances 0.000 claims abstract description 22
- 230000006835 compression Effects 0.000 claims abstract description 17
- 238000007906 compression Methods 0.000 claims abstract description 17
- 230000008961 swelling Effects 0.000 claims abstract description 17
- 238000007701 flash-distillation Methods 0.000 claims description 6
- 238000010025 steaming Methods 0.000 claims description 4
- 239000012263 liquid product Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract description 5
- 238000005516 engineering process Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 30
- 229930195733 hydrocarbon Natural products 0.000 description 7
- 150000002430 hydrocarbons Chemical class 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
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- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The utility model discloses a kind of mixed alkanes reaction product swell refrigeration piece-rate systems.System includes first-class heat exchanger, first throttle valve, second throttle, secondary heat exchanger, high pressure expansion power generator, inflated with low pressure generator, third throttle valve, high compression swelling discharge knockout drum, inflated with low pressure discharge knockout drum, 4th throttle valve, fluid product pumps, 5th throttle valve, fluid product flash tank, 6th throttle valve, reaction product second-stage separator, 7th throttle valve, reaction product primary separator, and fresh feed, reaction product, the pipelines such as gas phase isolate and liquid phase separation object；The utility model solves the problems, such as that the conventional hybrid alkane swell refrigeration separating technology C3+ rate of recovery is low, isolate purity is low, operability and adaptability are insufficient and high energy consumption, it realizes and reduces number of devices while ensureing dry gas high product purity, enhance device operability and adaptability, the C3/C4 rate of recovery is up to 99.92% in fluid product, heat exchange efficiency is high, and system energy consumption is low.
Description
Technical field
The utility model is related to chemical separating system more particularly to a kind of mixed alkanes reaction product swell refrigeration segregative lines
System.
Background technology
Reaction product piece-rate system is the key device of factory, determines the device capability, product recovery rate and energy of factory
Consumption.The piece-rate system mainly produces three kinds of products in the case where unstripped gas parameter is met the requirements：More rich in propylene and than it
Fluid product, dry gas product and the co-feeding of the hydro carbons of weight.For fluid product, which needs in unstripped gas
The heavy hydrocarbons such as most propane, propylene and iso-butane+isobutene are all separated, and the rate of recovery will could be protected 99.9% or more
Demonstrate,prove next workshop section's normal work.Include mainly the hydro carbons and hydrogen for being lighter than ethane from reaction product for dry gas product,
And a certain number of materials are extracted out from this burst of logistics as circulating air, purity determines the energy consumption of downstream separation hydrogen manufacturing, because
For the concentration requirement of this hydrogen 92.5% or more, the heavy hydrocarbons content of C3+ or more is less than 0.055%.It is third for co-feeding
Material needed for alkane dehydrogenation reactor, therefore, to assure that co-feeding can all gasify in piece-rate system
Using the peculiar effect of chemical industry equipment to distinctive mixture according to the difference pair of its physical property and chemical property
Its process detached is known as chemical separating, and the main technique mode that country's device uses at present has refrigerant cycle freeze, is swollen
Swollen refrigeration and hybrid refrigeration.For mixed alkanes reaction product, low energy consumption for import equipment, heat exchange efficiency is high, isolate purity is high,
But it is expensive, maintenance cost is high.The device to domesticize at present mostly uses greatly ISS (standard industry single-stage) swell refrigeration work
Skill, the mature technology, is widely used, but device driving situation is undesirable, and C3+ average recovery rates are relatively low, operability
Insufficient with adaptability, swell refrigeration technological process is single.
Invention content
The purpose of the utility model is to overcome the deficiencies in the prior art, provide a kind of mixed alkanes reaction product swell refrigeration
Piece-rate system.
The mixed alkanes reaction product swell refrigeration piece-rate system of the utility model, including first-class heat exchanger, first throttle
Valve, second throttle, secondary heat exchanger, high pressure expansion power generator, inflated with low pressure generator, third throttle valve, high compression swelling go out
Mouthful separator, inflated with low pressure discharge knockout drum, the 4th throttle valve, fluid product pump, the 5th throttle valve, fluid product flash tank,
6th throttle valve, reaction product second-stage separator, the 7th throttle valve, reaction product primary separator；
Reaction product pipeline is connect after first-class heat exchanger exchanges heat with reaction product primary separator；One fraction of reaction product
Liquid phase separation property management road from device lower part passes through the 7th throttle valve and enters first-class heat exchanger, then accesses fluid product flash distillation
Tank；The top of reaction product primary separator enters secondary heat exchanger heat exchange by reaction product pipeline, then access reaction production
Object second-stage separator；
The liquid phase separation property management road of reaction product second-stage separator lower part passes through the access fluid product flash distillation of the 6th throttle valve
The top of tank, reaction product second-stage separator enters secondary heat exchanger heat exchange by gas phase isolate pipeline, passes through after heat exchange
Then high pressure expansion power generator accesses high compression swelling discharge knockout drum；
The liquid phase separation property management road of high compression swelling discharge knockout drum lower part passes through the access fluid product flash distillation of the 5th throttle valve
Tank；Secondary heat exchanger is accessed in the top of high compression swelling discharge knockout drum by gas phase isolate pipeline, and in secondary heat exchanger
It is divided into tributary a and tributary b, tributary a is picked out from secondary heat exchanger, is then connect from dry gas products export after first-class heat exchanger
Go out；Tributary b from secondary heat exchanger pick out after by inflated with low pressure generator access inflated with low pressure discharge knockout drum；
The liquid phase separation property management road of inflated with low pressure discharge knockout drum lower part passes through the access fluid product flash distillation of the 4th throttle valve
Tank, inflated with low pressure discharge knockout drum top enter secondary heat exchanger by gas phase isolate pipeline, the conduct in secondary heat exchanger
Tributary c；
The top of fluid product flash tank first passes through secondary heat exchanger by gas phase isolate pipeline, is changed subsequently into level-one
Hot device, and picked out from flash distillation vapor outlet；The liquid phase separation property management road of fluid product flash tank lower part passes through fluid product pump access
Then first-class heat exchanger is picked out from fluid product discharge port；
Fresh feed pipeline enters first-class heat exchanger, is divided into mainstream and tributary d in first-class heat exchanger；Tributary d is changed from level-one
Hot device across first throttle valve enters back into first-class heat exchanger after picking out；Mainstream is divided into tributary e and branch after being picked out from first-class heat exchanger
F is flowed, tributary e enters first-class heat exchanger across second throttle, and tributary f then passes through third throttle valve again by secondary heat exchanger
Into secondary heat exchanger, and converging with the tributary c in secondary heat exchanger, the stream stock after converging accesses first-class heat exchanger,
Converge with tributary e and tributary d in first-class heat exchanger, and is picked out from co-feeding mouth.
Preferably, it is plate-fin heat exchanger that the first-class heat exchanger, which is the secondary heat exchanger described in plate-fin heat exchanger,.
Using the utility model, fresh feed carries out heat friendship in same heat exchanger with reaction product with cold material
It changes, the advantage that the logistics of plate-fin heat exchanger multiply can be given full play to while being exchanged heat, raising heat transfer temperature difference, C3/ in fluid product
The C4 rate of recovery is up to 99.92%；First-class heat exchanger is composed in parallel using four groups of heat exchange core bodies, and ice chest is piped full symmetric arrangement,
Heat exchange efficiency is greatly improved, system energy consumption is reduced；C3/C4 heavy hydrocarbons, second separation temperature are detached using two temperature spots
Degree point it is relatively low, can ensure dry gas product purity require while reduce number of devices, enhance device operability and
Adaptability；Stringent control operation temperature and pressure make co-feeding keep all gasifications；Overheated gas enters expansion unit expansion
Refrigeration, avoid saturated gas can energy band liquid enter expander inlet destroy expander inlet guide vane wheel the problem of, improve swollen
The stability of swollen machine.
Description of the drawings
Fig. 1 is mixed alkanes reaction product swell refrigeration piece-rate system schematic diagram；
Fig. 2 is first-class heat exchanger inlet port and outlet port distribution schematic diagram；
Fig. 3 is secondary heat exchanger inlet port and outlet port distribution schematic diagram.
In figure, first-class heat exchanger 1, first throttle valve 2, second throttle 3, secondary heat exchanger 4, high pressure expansion power generator 5,
Inflated with low pressure generator 6, third throttle valve 7, high compression swelling discharge knockout drum 8, inflated with low pressure discharge knockout drum the 9, the 4th throttle
Valve 10, fluid product pump the 11, the 5th throttle valve 12, fluid product flash tank 13, the 6th throttle valve 14, reaction product the second-order separation
Device 15, the 7th throttle valve 16, reaction product primary separator 17.
Specific implementation mode
As shown in Figures 2 and 3, the first-class heat exchanger 1 and two level respectively illustrated in one embodiment of the utility model is changed
Each discharge port of hot device 4 and the position of feed inlet.
With reference to Fig. 1-Fig. 3, the utility model is described further.
A kind of mixed alkanes reaction product swell refrigeration piece-rate system in the utility model embodiment, including level-one heat exchange
Device 1, first throttle valve 2, second throttle 3, secondary heat exchanger 4, high pressure expansion power generator 5, inflated with low pressure generator 6, third
Throttle valve 7, high compression swelling discharge knockout drum 8, inflated with low pressure discharge knockout drum 9, the 4th throttle valve 10, fluid product pump 11, the
It is five throttle valves 12, fluid product flash tank 13, the 6th throttle valve 14, reaction product second-stage separator 15, the 7th throttle valve 16, anti-
Product primary separator 17, fresh feed pipeline, reaction product pipeline, gas phase isolate pipeline and liquid phase separation property management road are answered,
The first-class heat exchanger 1 and secondary heat exchanger 4 is plate-fin heat exchanger；
Reaction product pipeline is accessed from the first charging aperture of first-class heat exchanger 1, is picked out from the 6th discharge port, and is produced with reacting
Object primary separator 17 connects；The liquid phase separation property management road of 17 lower part of reaction product primary separator pass through the 7th throttle valve 16 from
The third feed inlet of first-class heat exchanger 1 accesses, and is picked out from the 5th discharge port, then accesses fluid product flash tank 13；Reaction production
The top of object primary separator 17 is accessed by reaction product pipeline from the first charging aperture of secondary heat exchanger 4, from the 6th discharging
Mouth picks out, and then accesses reaction product second-stage separator 15；
The liquid phase separation property management road of 15 lower part of reaction product second-stage separator passes through the 6th throttle valve 14 to access fluid product
Flash tank 13, upper part by gas phase isolate pipeline from the 4th feed inlet of secondary heat exchanger 4 access, and from its 7th discharging
Mouth picks out, and then high compression swelling discharge knockout drum 8 is accessed by high pressure expansion power generator 5；
The liquid phase separation property management road of high 8 lower part of compression swelling discharge knockout drum passes through the 5th throttle valve 12 access fluid product to dodge
Steaming pot 13；The 5th charging of secondary heat exchanger 4 is accessed on the top of high compression swelling discharge knockout drum 8 by gas phase isolate pipeline
Mouthful, one tributary a picks out from the second discharge port, then accesses the 5th feed inlet of first-class heat exchanger 1, and from its second discharge port
It picks out；Another tributary b is picked out from the 6th discharge port of secondary heat exchanger 4, and accessing inflated with low pressure by inflated with low pressure generator 6 goes out
Mouth separator 9；
The liquid phase separation property management road of 9 lower part of inflated with low pressure discharge knockout drum passes through the 4th throttle valve 10 access fluid product to dodge
Steaming pot 13, upper part is accessed by gas phase isolate pipeline from the 6th feed inlet of secondary heat exchanger 4, as tributary c；
The top of fluid product flash tank 13 is connect by gas phase isolate pipeline from the third feed inlet of secondary heat exchanger 4
Enter, picked out from the first discharge port, then access the 4th feed inlet of first-class heat exchanger 1, and is picked out from its first discharge port；Liquid
The liquid phase separation property management road of 13 lower part of product flash tank passes through the 7th feed inlet of 11 access first-class heat exchanger 1 of fluid product pump,
Then it is picked out from its 4th discharge port；
Fresh feed pipeline is accessed from the second charging aperture of first-class heat exchanger 1, and one tributary d is picked out from the 8th discharge port,
The 8th feed inlet is accessed across first throttle valve 2；Another tributary is picked out from the 7th discharge port, and then a tributary e passes through the second section
It flowing valve 3 and accesses the 9th feed inlet, another tributary f is accessed from the second charging aperture of secondary heat exchanger 4, is picked out from the 5th discharge port,
It then passes through third throttle valve 7 and accesses its 7th feed inlet, converge with tributary c, and picked out from third discharge port, then access one
6th feed inlet of grade heat exchanger 1, then converge with tributary e and tributary d, and picked out from third discharge port.
A kind of 6th feed inlet of the first-class heat exchanger 1 of mixed alkanes reaction product swell refrigeration piece-rate system, the 8th into
Material mouth and the 9th feed inlet pick out after converging inside first-class heat exchanger 1 from third discharge port.
A kind of 6th feed inlet of the secondary heat exchanger 4 of mixed alkanes reaction product swell refrigeration piece-rate system and the 7th into
Material mouth picks out after converging inside secondary heat exchanger 4 from third discharge port.
As shown in Figures 1 to 3, a kind of mixed alkanes reaction product swell refrigeration separating technology side as described in claim 1
Method includes the following steps：
1) reaction product and fresh feed enter first-class heat exchanger 1 as heat from first charging aperture and second charging aperture respectively
It flows, the co-feeding, dry gas product, fluid product, flashed vapour in first-class heat exchanger 1 are as cold flow, and cold flow is with hot-fluid in level-one
Heat exchange is carried out in heat exchanger 1, the reaction product after being condensed enter in reaction product primary separator 17 carry out gas phase with
Liquid phase separation, the part fresh feed after being condensed enter secondary heat exchanger 4 by tributary f；
2) the gas phase isolate separated from reaction product primary separator 17 and secondary heat exchange is entered by tributary f
The fresh feed of device 4 is as hot-fluid, co-feeding, dry gas product, high pressure expansion machine logistics gas, cycle in secondary heat exchanger 4
Hydrogen carries out heat exchange with hot-fluid as cold flow, cold flow in secondary heat exchanger 4, is entered by condensed reaction product again
Gas phase and liquid phase separation are carried out in reaction product second-stage separator 15；
3) the gas phase isolate separated from reaction product second-stage separator 15 enters two level by the 4th feed inlet
Heat exchanger 4 heats, and then entering high pressure expansion power generator 5 as logistics carries out swell refrigeration；Logistics after expansion enters high pressure
It expands discharge knockout drum 8 and carries out gas phase and liquid phase separation, the gas phase isolate part isolated enters tributary a and produced as dry gas
Product heat in secondary heat exchanger 4, and go out secondary heat exchanger 4 from the second discharge port, and then entering level-one from the 5th feed inlet changes
1 re-heat of hot device, and flowed out from its second discharge port, another part gas phase isolate enters tributary b as circulating hydrogen in two level
Then re-heat in heat exchanger 4 enters inflated with low pressure generator 6 as logistics and carries out swell refrigeration, the logistics after expansion enters low
Compression swelling discharge knockout drum 9 carries out gas phase and liquid phase separation, the gas phase isolate isolated and enters tributary c, and new in the f of tributary
Fresh raw material mixing, the co-feeding as premixing are that secondary heat exchanger 4 provides cold flow；
4) co-feeding being pre-mixed goes out secondary heat exchanger 4 from third discharge port, then enters level-one from the 6th feed inlet
Heat exchanger 1, then mixed with the fresh feed in tributary e and tributary d and be used as co-feeding, cold flow is provided for first-class heat exchanger 1, and
It is flowed out from third discharge port；
5) high compression swelling discharge knockout drum 8, inflated with low pressure discharge knockout drum 9, reaction product second-stage separator 15 and reaction
Liquid phase separation object in product primary separator 17 passes through the 5th throttle valve 12, the 4th throttle valve 10, the 6th throttle valve 14 respectively
With after 16 reducing pressure by regulating flow of the 7th throttle valve enter fluid product flash tank 13；The flash steam isolated in fluid product flash tank 13
Successively through secondary heat exchanger 4 and 1 re-heat of first-class heat exchanger at normal outflow；The liquid phase separation isolated in fluid product flash tank 13
Object enters 1 re-heat of first-class heat exchanger at room temperature, as liquid product flow after 11 pressurization of fluid product pump from the 7th feed inlet
Go out.
Another specific embodiment according to the present utility model, first-class heat exchanger 1 and two level described in the utility model are changed
Reaction product in hot device 4 is the steam stream containing hydrogen and hydrocarbon mixture, and temperature is 42~50 DEG C, pressure is 1~
1.08MPa；Fresh feed in the first-class heat exchanger 1 and secondary heat exchanger 4 is liquid hydrocarbon, pressure is 1.02~
1.1MPa；Operation -30~-20 DEG C in the fluid product pump 11, operating pressure are 4.4~4.5MPa；The two level
The co-feeding of premixing in heat exchanger 4 and the temperature of the co-feeding in first-class heat exchanger 1 are 40~50 DEG C, and pressure is
0.27~0.28MPa；Operation temperature is -40~-60 DEG C in the reaction product primary separator 17, the reaction product
Operation temperature is -100~-125 DEG C in second-stage separator 15；The high pressure expansion power generator 5 is expansion power generation pattern, power generation
Amount is 450~550kW, and operating pressure is 10 to 6 kilograms of gauge pressures, and the inflated with low pressure generator 6 is also expansion power generation pattern,
Generated energy is 450~550kW, and operating pressure is 6 to 4 kilograms of gauge pressures.
Claims (3)
1. a kind of mixed alkanes reaction product swell refrigeration piece-rate system, it is characterised in that including first-class heat exchanger (1), first segment
Flow valve (2), second throttle (3), secondary heat exchanger (4), high pressure expansion power generator (5), inflated with low pressure generator (6), third
Throttle valve (7), high compression swelling discharge knockout drum (8), inflated with low pressure discharge knockout drum (9), the 4th throttle valve (10), fluid product
Pump (11), the 5th throttle valve (12), fluid product flash tank (13), the 6th throttle valve (14), reaction product second-stage separator
(15), the 7th throttle valve (16), reaction product primary separator (17)；
Reaction product pipeline is connect after first-class heat exchanger (1) heat exchange with reaction product primary separator (17)；Reaction product one
The liquid phase separation property management road of grade separator (17) lower part passes through the 7th throttle valve (16) and enters first-class heat exchanger (1), then connects
Enter fluid product flash tank (13)；The top of reaction product primary separator (17) enters secondary heat exchange by reaction product pipeline
Device (4) exchanges heat, and then accesses reaction product second-stage separator (15)；
The liquid phase separation property management road of reaction product second-stage separator (15) lower part passes through the 6th throttle valve (14) to access fluid product
Flash tank (13), the top of reaction product second-stage separator (15) enter secondary heat exchanger (4) by gas phase isolate pipeline and change
Heat passes through high pressure expansion power generator (5) and then the high compression swelling discharge knockout drum (8) of access after heat exchange；
The liquid phase separation property management road of high compression swelling discharge knockout drum (8) lower part passes through the 5th throttle valve (12) access fluid product to dodge
Steaming pot (13)；The top of high compression swelling discharge knockout drum (8) by gas phase isolate pipeline access secondary heat exchanger (4), and
It is divided into tributary a and tributary b in secondary heat exchanger (4), tributary a is picked out from secondary heat exchanger (4), then passes through first-class heat exchanger
(1) it is picked out from dry gas products export after；Tributary b from secondary heat exchanger (4) pick out after by inflated with low pressure generator (6) access it is low
Compression swelling discharge knockout drum (9)；
The liquid phase separation property management road of inflated with low pressure discharge knockout drum (9) lower part passes through the 4th throttle valve (10) access fluid product to dodge
Steaming pot (13), inflated with low pressure discharge knockout drum (9) top enters secondary heat exchanger (4) by gas phase isolate pipeline, in two level
Tributary c is used as in heat exchanger (4)；
The top of fluid product flash tank (13) first passes through secondary heat exchanger (4) by gas phase isolate pipeline, subsequently into one
Grade heat exchanger (1), and picked out from flash distillation vapor outlet；The liquid phase separation property management road of fluid product flash tank (13) lower part passes through liquid
Product pump (11) accesses first-class heat exchanger (1), is then picked out from fluid product discharge port；
Fresh feed pipeline enters first-class heat exchanger (1), is divided into mainstream and tributary d in first-class heat exchanger (1)；Tributary d is from level-one
Heat exchanger (1) across first throttle valve (2) enters back into first-class heat exchanger (1) after picking out；Mainstream is after first-class heat exchanger (1) picks out
It is divided into tributary e and tributary f, tributary e passes through second throttle (3) to enter first-class heat exchanger (1), and tributary f passes through secondary heat exchanger
(4) it then passes through third throttle valve (7) and enters back into secondary heat exchanger (4), and the tributary c interior and described in secondary heat exchanger (4)
Converge, stream stock after converging access first-class heat exchanger (1) is converged in first-class heat exchanger (1) with tributary e and tributary d, and from connection
Feed inlet is closed to pick out.
2. mixed alkanes reaction product swell refrigeration piece-rate system according to claim 1, it is characterised in that described one
Grade heat exchanger (1) is plate-fin heat exchanger.
3. mixed alkanes reaction product swell refrigeration piece-rate system according to claim 1, it is characterised in that described two
Grade heat exchanger (4) is plate-fin heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820060795.9U CN207751220U (en) | 2018-01-15 | 2018-01-15 | A kind of mixed alkanes reaction product swell refrigeration piece-rate system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820060795.9U CN207751220U (en) | 2018-01-15 | 2018-01-15 | A kind of mixed alkanes reaction product swell refrigeration piece-rate system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207751220U true CN207751220U (en) | 2018-08-21 |
Family
ID=63151758
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820060795.9U Withdrawn - After Issue CN207751220U (en) | 2018-01-15 | 2018-01-15 | A kind of mixed alkanes reaction product swell refrigeration piece-rate system |
Country Status (1)
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108036583A (en) * | 2018-01-15 | 2018-05-15 | 杭州中泰深冷技术股份有限公司 | A kind of mixed alkanes reaction product swell refrigeration piece-rate system and its method |
-
2018
- 2018-01-15 CN CN201820060795.9U patent/CN207751220U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108036583A (en) * | 2018-01-15 | 2018-05-15 | 杭州中泰深冷技术股份有限公司 | A kind of mixed alkanes reaction product swell refrigeration piece-rate system and its method |
| CN108036583B (en) * | 2018-01-15 | 2023-12-01 | 杭州中泰深冷技术股份有限公司 | Mixed alkane reaction product expansion refrigeration separation system and method thereof |
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