CN204830683U - Polypropylene tail gas recovery unit - Google Patents
Polypropylene tail gas recovery unit Download PDFInfo
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- CN204830683U CN204830683U CN201520563229.6U CN201520563229U CN204830683U CN 204830683 U CN204830683 U CN 204830683U CN 201520563229 U CN201520563229 U CN 201520563229U CN 204830683 U CN204830683 U CN 204830683U
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Abstract
The utility model discloses a polypropylene tail gas recovery unit, including compression unit, dry unit, membrane separation unit and the cryogenic separation unit that connects gradually, the compression unit is including at least one compressor, a heat exchanger and vapour and liquid separator who connects gradually, dry unit, including two at least adsorption towers that connect gradually, the drier is equipped with in the adsorption tower, the membrane separation unit is including the membrane separator, the cryogenic separation unit is including at least one high -efficient multichannel heat exchanger, at least one low temperature vapour and liquid separator, at least one gas expansion equipment and at least one liquid bloating plant. The utility model discloses polypropylene tail gas is retrieved through the cryogenic method of inflation for propylene liquefaction in the polypropylene tail gas realizes the recovery of propylene, purifies nitrogen gas simultaneously, satisfies the requirement that nitrogen gas recycled, combine membrane separation technique, hydrogen in the desorption polypropylene tail gas, the rate of recovery of propylene more than 98% in the realization polypropylene tail gas.
Description
Technical field
The utility model relates to polyolefin field, be specifically related to a kind of in polypropylene production process propylene and nitrogen gas recovering apparatus in emission.
Background technology
In polypropylene production process, in refining, the polymerisation and acrylic resin degasification process of propylene monomer, the tail gas containing a large amount of propylene monomer all can be had to discharge.As deviate from from degassing tower tower top in propylene refining process shallow bid light component stream, in order to control inert gas content polymerization process reaction periodic off-gases, adopt nitrogen+mixture of steam to send into bottom degassing cabin, to remove hydrocarbon and the de-storehouse tail gas etc. making residual catalyst inactivation and produce.These gases are referred to as polypropylene tail gas, its main component is nitrogen, propylene and a small amount of propane, ethane, ethene, water etc., the concentration of general propylene is in 6 ~ 50% (V) left and right, scale is the polypropylene plant of 300,000 tons/year, the propylene contained in tail gas nearly annual 3000 tons, nitrogen more than 5000 ton, so the hydro carbons reclaimed in tail gas and nitrogen have very high economic benefit.
US Patent No. Patent5769927 proposes the process of the method process polypropylene tail gas adopting compression, condensation and UF membrane integrated.Flow process is as described below.First polypropylene tail gas is carried out supercharging, then through condenser, gas temperature is dropped to below dew point, a part of propylene becomes liquid, separates; The propylene that another part is in gas phase enters into UF membrane part, utilizes film preferentially to permeate the feature of propylene, and make propylene and nitrogen realize being separated, the Rich propylene body obtained turns back to compression condensation part, further Propylene recovery.This process can realize the recycling of propylene and nitrogen, but because the Rich propylene body of film turns back to compression condensation part, the tolerance of the compression after circulation and condensation is caused to be 1.5 ~ 3 times of initial ejection tolerance, the investment of compression and refrigeration plant and energy consumption are all significantly increased, reduces the economy of this process.
Chinese patent CN101357291B discloses, and adopts absorption at normal temperatures and pressures to obtain high purity product nitrogen, desorption under negative pressure, then by desorption gas compression condensation, obtains highly purified product propylene liquid.But the method needs to adopt vavuum pump to resolve adsorption tower, two compressors are at least needed to carry out supercharging to the hydrocarbon gas reclaimed and nitrogen respectively, dynamic equipment is many, complicated operation, vacuum analysis process easily causes Air infitration recovery system, there is potential safety hazard, when containing certain density hydrogen in discharge gas, adsorption process can not realize the separation of the hydrogen of nitrogen, cause nitrogen not recycle, can only torch be discharged into, cause the wasting of resources, and environmental pollution, the floor space of equipment is large simultaneously.
Utility model content
In view of the problems referred to above existing for prior art, the utility model aims to provide the polypropylene tail gas recovery device that process is simple, energy consumption is low, small investment, floor space are little that a kind of propylene recovery rate is high, nitrogen can reuse.
The utility model object is to provide a kind of polypropylene tail gas recovery device, and described device comprises:
Compression unit, comprises at least one compressor, a heat exchanger and a gas-liquid separator.For improving the pressure of polypropylene tail gas, meet the operating pressure requirement of swell refrigeration, cryogenic separation and UF membrane, simultaneously by compression after gas be cooled to normal temperature, and in gas-liquid separator separating and condensing high boiling liquid out, obtain the compressed air stream of lime set stream and normal temperature.
Drying unit, comprises at least two adsorption towers, and tower, built with drier, for the treatment of the normal temperature compressed gas exported from compression unit, removes the moisture in gas, obtains dry air-flow.
Film separation unit, comprises membrane separator and Hydrogen Separation film, for the treatment of the air-flow exported from drying unit, isolates the hydrogen in gas, obtains hydrogen-depleted gas stream.
Cryogenic separation unit: comprise at least one efficient multi-channel heat exchanger, at least one low temperature gas-liquid separator, at least one gas expansion equipment and at least one expansion of liquids equipment.Described membrane separator outlet connects hot media channel C-C, the low temperature gas-liquid separator entrance of efficient multi-channel heat exchanger successively; Low temperature gas-liquid separator outlet at bottom is connecting fluid volume expansion equipment, the cold medium channel D-D of efficient multi-channel heat exchanger, pipeline k successively; Low temperature gas-liquid separator top exit connects cold medium channel A-A, the gas expansion equipment of efficient multi-channel heat exchanger successively, the cold medium channel B-B of efficient multi-channel heat exchanger, pipeline o; For the treatment of the hydrogen-depleted gas stream exported from film separation unit, by the heat exchange of swell refrigeration, multi-fluid, the temperature of gas is reduced further, realize the liquefaction of propylene, through gas-liquid separation, the propylene stream be recycled and nitrogen stream.
Further, in technique scheme, in drying unit, described drier is selected from activated alumina, silica gel, molecular sieve.
Further, in technique scheme, described Hydrogen Separation film refers to relative to hydro carbons, nitrogen, can the various diffusion barriers of preferential permeated hydrogen, as macromolecular material diffusion barriers such as polyimides, polysulfones, Nomex, acetate fiber, polyphenylene oxide, or the metal film such as palladium film.
Further, in technique scheme, described bloating plant refers to a kind of refrigeration plant pressure energy of fluid being converted to cold, and described expansion of liquids equipment is selected from throttle expansion valve.
Described gas expansion equipment is selected from turbo-expander, air wave refrigerating device.
Further, in technique scheme, described efficient multi-channel heat exchanger refers to plate-fin heat exchanger or around heat exchange of heat pipe.
Device of the present utility model is by the organic assembling of compression unit, drying unit, film separation unit and cryogenic separation unit, and effectively can reclaim the propylene in tail gas and nitrogen, the rate of recovery of propylene is more than 98%, and the nitrogen gas purity of recovery is more than 97.5%.
Another object of the present utility model there is provided a kind of method utilizing described polypropylene tail gas recovery device Propylene recovery and nitrogen, and it comprises the steps:
Compression step, first the pressure of gas is elevated to 0.6 ~ 3.0MPaA through compressor by polypropylene tail gas, then through heat exchanger, the temperature of the high-temperature gas after compression is dropped to normal temperature, cooling medium adopts recirculated water, cooled gas carries out gas-liquid separation in gas-liquid separator, high boiling component in tail gas, becomes liquid phase as water and heavy hydrocarbon have portion, discharges from the bottom of gas-liquid separator as lime set.
Drying steps, from gas-liquid separator, gas phase out enters dehydration adsorption tower, and the moisture in removing discharge gas, drops to less than-30 ~-130 DEG C by water dew point.
UF membrane step, the gas after dehydrating enters membrane separator, and built with Hydrogen Separation film, the characteristic of film is preferential through hydrogen component, can by the Hydrogen Separation in tail gas out, and the hydrogen-rich gas of infiltration is discharged into torch.The gas removing most of hydrogen enters cryogenic separation step.
Cryogenic separation step, the gas removing most of hydrogen enters into efficient multi-channel heat exchanger and cools step by step, one or one or more hot media channel and one or the cold medium channel of one or more is provided with in heat exchanger, after heat exchanger, the temperature of gas is reduced to-30 ~-130 DEG C, then enter low temperature gas-liquid separator and carry out gas-liquid separation, the liquid propene obtained is after the decompression of expansion of liquids equipment, turn back to efficient multi-channel heat exchanger, the propylene of gas phase is flashed to by low temperature gas-liquid separator gas out after exchanging cold, its composition is mainly nitrogen, turn back to efficient multi-channel heat exchanger, reclaim after cold through re-heat and reclaim.
Further, in technique scheme, enter bloating plant through the re-heat nitrogen reclaimed after cold and carry out swell refrigeration, cryogenic gas after expansion turns back to efficient multi-channel heat exchanger again, for whole system provides cold, this gas, after re-heat, as the nitrogen reclaimed, returns polypropylene plant and reuses.
Further, in technique scheme, the propylene of recovery can directly be sent to or be sent to ethylene unit after supercharging, then is the propylene of polymer grade by propylene refining; The way of compression condensation can also be adopted to be liquefied by gas-phase propene, make liquid propene.
Utility model beneficial effect
1) by the method for swell refrigeration, the propylene in polypropylene tail gas is liquefied, realizes the recovery of propylene, simultaneously nitrogen purge gas, meet the requirement that nitrogen circulation uses;
2) binding film isolation technics, removes the hydrogen in polypropylene tail gas;
3) realize the rate of recovery of propylene more than 98% in polypropylene tail gas, far above the propylene recovery rate of prior art, greatly reduce the unit consumption of polypropylene plant;
4) equipment is thrown few, and operation energy consumption is low, floor space is little.
Accompanying drawing explanation
Fig. 1 is the system diagram of the utility model polypropylene tail gas recovery device and method;
In figure, 100, compression unit; 110, tail-gas compressor; 120, water recirculator; 130, normal temperature gas-liquid separator; 200, drying unit; 201, adsorption tower; 300, membrane separator unit; 310, membrane separator; 400, cryogenic separation unit; 410, efficient multi-channel heat exchanger; 420, low temperature gas-liquid separator; 430, expansion of liquids equipment; 440, gas expansion equipment; 10, pipeline a; 11, pipeline b; 12, pipeline c; 13, pipeline d; 14, pipeline e; 15, pipeline j; 16, pipeline h; 17, pipeline i; 18, pipeline j; 19, pipeline k; 20, pipeline l; 21, pipeline m; 22, pipeline n; 23, pipeline o; 24, pipeline f; 29, pipeline p.
Detailed description of the invention
Now by reference to the accompanying drawings, the utility model is described in further detail.
As shown in Figure 1, a kind of polypropylene tail gas recovery device that the utility model provides comprises:
Compression unit 100, comprises a tail-gas compressor 110, water recirculator 120 and normal temperature gas-liquid separator 130.Tail gas in polypropylene production process, is connected to the entrance of tail-gas compressor 110 by pipeline a10.The pressure of gas is elevated to 0.6 ~ 3.0MPaA by tail-gas compressor 110, meets the operating pressure requirement of swell refrigeration, cryogenic separation and UF membrane.Gas after compression is connected to water recirculator 120 by pipeline b11, and the gas after compression is cooled to normal temperature, and be connected to normal temperature gas-liquid separator 130 by pipeline c12 and carry out gas-liquid separation, the lime set obtained bottom it is by pipeline p29 carrying device; The unheated air obtained at its top enters drying unit 200 by pipeline d13.
Drying unit 200 comprises the adsorption tower 210 being equipped with and dehydrating agent, and the quantity of adsorption tower 201, according to the process size of tolerance and the regeneration gas of selection, is set to 2,3 or 4.After adsorption tower 210, the water dew point of gas is reduced to-30 ~-130 DEG C, then enters membrane separator unit 300 by pipeline e14.
Membrane separator unit 300 comprises the membrane separator 310 that membrane module is housed, when the air-flow that drying unit exports is by membrane separator 310, hydrogen is preferentially through penetrating through film, the hydrogen rich stream of low pressure is obtained in the per-meate side of film, be discharged into torch by pipeline f24, hydrogen-depleted gas flows through pipeline g15 and enters cryogenic separation unit 400.
Cryogenic separation unit 400 comprises an efficient multi-channel heat exchanger 410, low temperature gas-liquid separator 420, gas expansion equipment 440 and an expansion of liquids equipment 430.The hydrogen-depleted gas exported from film separation unit 300 flows through pipeline g15, enter efficient multi-channel heat exchanger 410, the preferred plate-fin heat exchanger of the utility model, after hot media channel C-C, the temperature of gas drops to-30 ~-130 DEG C gradually, low temperature gas-liquid separator 420 is entered by pipeline h16, carry out gas-liquid separation, the propylene be recycled bottom low temperature gas-liquid separator 420, this liquid propene is through pipeline i17 connecting fluid volume expansion equipment 430, the preferred throttle expansion valve of the utility model, this strand of liquid temperature and pressure after throttling expansion reduces, then efficient multi-channel heat exchanger 410 is returned by pipeline j18, heat exchange is carried out with thermal medium, cold is provided, after cold medium channel D-D, the propylene stream be recycled, device is transferred out through pipeline k19, can directly be sent to or be sent to ethylene unit after supercharging, be the propylene of polymer grade by propylene refining again, the way of compression condensation can also be adopted to be liquefied by gas-phase propene, make liquid propene.The on-condensible gas at low temperature gas-liquid separator 420 top, mainly nitrogen, efficient multi-channel heat exchanger 410 is turned back to by pipeline l20, heat exchange is carried out with thermal medium, cold is provided, after cold medium channel A-A, gas expansion equipment 440 is entered by pipeline m21, carry out swell refrigeration, the preferred turbo-expander of gas expansion equipment in the utility model, the cryogenic gas obtained after turbine expansion, efficient multi-channel heat exchanger 410 is turned back to by pipeline n22, heat exchange is carried out with thermal medium, cold is provided, after cold medium channel B-B, the nitrogen stream be recycled, by pipeline o23 carrying device, turn back to polypropylene plant recycling.
In a preferred embodiment of the present utility model, according to the pressure of gas and the difference of tolerance, gas expansion equipment 440 can adopt turbo-expander series connection or the parallel operation of more than one or one, thus provides more cold for cryogenic separation unit.
The utility model additionally provides a kind of method utilizing described polypropylene tail gas recovery device Propylene recovery and nitrogen, below in conjunction with accompanying drawing and embodiment, the utility model is described in further detail, those of ordinary skill in the art's comprehend the utility model can be made, but limit the utility model never in any form.Pressure described in literary composition is gauge pressure.
Embodiment 1
In the polypropylene tail gas shown in Fig. 1 Propylene recovery and nitrogen process flow diagram in, the pressure of polypropylene tail gas is 0.05MPa, and temperature is 50 DEG C, and tolerance is 1000Nm
3/ hr, composed as follows:
| Component | H 2 | Propylene | Propane | Ethene | Hexane | H 2O | N 2 |
| Content %V/V | 1.28 | 8.10 | 0.10 | 6.50 | 0.25 | 0.27 | 83.50 |
First this tail gas enter compression unit 100, and the pressure of gas is elevated to 1.6MPa by tail-gas compressor 110, then enters water recirculator 120, and the gas after compression is cooled to 40 DEG C.Cooled gas enters normal temperature gas-liquid separator 130 and carries out gas-liquid separation, the lime set carrying device obtained bottom it; The unheated air obtained at its top enters drying unit 200.At drying unit, gas is by adsorption tower, and adsorbent is the multiple-hearth of activated alumina and molecular sieve composition, by H
2o content drops to below 1ppmv, prevents that ice occurs in follow-up cryogenic separation process and blocks up.Dried gas enters membrane separator unit 300, and membrane separator is equipped with membrane module, and its membrane material used is polyimides, and after diffusion barrier, obtain the infiltration gas logistics of film, its pressure is 0.05MPa, and temperature is 40 DEG C, and tolerance is 33Nm
3/ hr, composed as follows:
| Component | H 2 | Propylene | Propane | Ethene | Hexane | H 2O | N 2 |
| Content %V/V | 14.82 | 3.23 | 0.02 | 4.94 | 0.04 | 0.00 | 76.95 |
The logistics of this strand of infiltration gas is discharged into torch; The side that retains of UF membrane is that hydrogen-depleted gas flows to into cryogenic separation unit 400.
First hydrogen-depleted gas stream enter plate-fin heat exchanger, after hot media channel C-C, the temperature of gas drops to-120 DEG C gradually, now the propylene of more than 99% has all liquefied, then at low temperature gas-liquid separator 420, carry out gas-liquid separation, the propylene be recycled bottom low temperature gas-liquid separator 420, this liquid propene is through throttle expansion valve, after expanding, temperature and pressure reduces, then Returning plate fin heat exchanger, heat exchange is carried out with thermal medium, cold is provided, after cold medium channel D-D, the propylene stream be recycled, its pressure is 0.25MPa, temperature is 30 DEG C, tolerance is 143Nm
3/ hr, composed as follows:
| Component | H 2 | Propylene | Propane | Ethene | Hexane | H 2O | N 2 |
| Content %V/V | 0.005 | 55.778 | 0.728 | 37.428 | 1.726 | 0.000 | 4.336 |
This strand of air-flow is directly sent to ethylene unit, then is the propylene of polymer grade by propylene refining.
The on-condensible gas at low temperature gas-liquid separator 420 top, mainly nitrogen, turn back to plate-fin heat exchanger 410, carry out heat exchange with thermal medium, cold is provided, after cold medium channel A-A, enter turbo-expander, carry out swell refrigeration, in the present embodiment, adopt a decompressor, single-stage expansion, the cryogenic gas obtained after turbine expansion, turns back to plate-fin heat exchanger, carries out heat exchange with thermal medium, cold is provided, after cold medium channel B-B, the nitrogen stream be recycled, its pressure is 0.22MPa, temperature is 20 DEG C, and tolerance is 821Nm
3/ hr, composed as follows:
| Component | H 2 | Propylene | Propane | Ethene | Hexane | H 2O | N 2 |
| Content %V/V | 0.96 | 0.04 | 0.00 | 1.21 | 0.00 | 0.00 | 97.79 |
According to actual conditions, it can be turned back in whole or in part polypropylene plant recycling.
Embodiment 2
In the polypropylene tail gas shown in Fig. 1 Propylene recovery and nitrogen process flow diagram in, the pressure of polypropylene tail gas is 0.02MPa, and temperature is 51 DEG C, and tolerance is 900Nm
3/ hr, composed as follows:
| Component | H 2 | Propylene | Propane | Ethene | Hexane | H 2O | N 2 |
| Content %V/V | 0.60 | 27.67 | 5.55 | 1.40 | 0.00 | 0.99 | 63.79 |
First this tail gas enter compression unit 100, and the pressure of gas is elevated to 1.7MPa by tail-gas compressor 110, then enters water recirculator 120, and the gas after compression is cooled to 40 DEG C.Cooled gas enters normal temperature gas-liquid separator 130 and carries out gas-liquid separation, and the lime set obtained bottom it passes through carrying device; The unheated air obtained at its top enters drying unit 200.At drying unit, gas is by adsorption tower, and adsorbent is the multiple-hearth of activated alumina and molecular sieve composition, by H
2o content drops to below 1ppmv, prevents that ice occurs in follow-up cryogenic separation process and blocks up.Dried gas enters membrane separator unit 300, and membrane separator is equipped with membrane module, and its membrane material used is polyimides, and after diffusion barrier, obtain the infiltration gas logistics of film, its pressure is 0.05MPa, and temperature is 38 DEG C, and tolerance is 38Nm
3/ hr, composed as follows:
| Component | H 2 | Propylene | Propane | Ethene | Hexane | H 2O | N 2 |
| Content %V/V | 6.72 | 14.45 | 1.58 | 1.38 | 0.00 | 0.00 | 75.86 |
The logistics of this strand of infiltration gas is discharged into torch; The side that retains of UF membrane is that hydrogen-depleted gas flows to into cryogenic separation unit 400.
First hydrogen-depleted gas stream enter plate-fin heat exchanger, after hot media channel C-C, the temperature of gas drops to-110 DEG C gradually, now the propylene of more than 99% has all liquefied, then at low temperature gas-liquid separator 420, carry out gas-liquid separation, the propylene be recycled bottom low temperature gas-liquid separator 420, this liquid propene is through throttle expansion valve, after expanding, temperature and pressure reduces, then Returning plate fin heat exchanger, heat exchange is carried out with thermal medium, cold is provided, after cold medium channel D-D, the propylene stream be recycled, its pressure is 0.05MPa, temperature is 25 DEG C, tolerance is 314Nm
3/ hr, composed as follows:
| Component | H 2 | Propylene | Propane | Ethene | Hexane | H 2O | N 2 |
| Content %V/V | 0.00 | 77.27 | 15.66 | 3.50 | 0.00 | 0.00 | 3.57 |
This strand of air-flow needs to be sent to ethylene unit by further supercharging, then is the propylene of polymer grade by propylene refining.
The on-condensible gas at low temperature gas-liquid separator 420 top, mainly nitrogen, turn back to plate-fin heat exchanger, carry out heat exchange with thermal medium, cold is provided, after cold medium channel A-A, enter turbo-expander, carry out swell refrigeration, adopt two decompressor serial operations in the present embodiment, the cryogenic gas obtained after turbine expansion, turn back to plate-fin heat exchanger, carry out heat exchange with thermal medium, cold is provided, after cold medium channel B-B, the nitrogen stream be recycled, its pressure is 0.25MPa, and temperature is 15 DEG C, and tolerance is 5381Nm
3/ hr, composed as follows:
| Component | H 2 | Propylene | Propane | Ethene | Hexane | H 2O | N 2 |
| Content %V/V | 0.52 | 0.14 | 0.02 | 0.21 | 0.00 | 0.00 | 99.11 |
It according to actual conditions, can be turned back to polypropylene plant recycling by nitrogen stream in whole or in part.
From embodiment provided by the utility model, method of the present utility model can reclaim propylene in polypropylene tail gas and nitrogen preferably, and make the rate of recovery of propylene in tail gas be greater than 98%, nitrogen gas purity is more than 97.5%.In addition, pressure energy is also converted into low temperature cold by turbine expansion equipment by method of the present utility model, and capacity usage ratio is high, cost of investment is low, be easy to the advantages such as operation.
The above; be only the utility model preferably detailed description of the invention; but protection domain of the present utility model is not limited thereto; anyly be familiar with those skilled in the art in the technical scope that the utility model discloses; be equal to according to the technical solution of the utility model and utility model design thereof and replace or change, all should be encompassed within protection domain of the present utility model.
Claims (6)
1. a polypropylene tail gas recovery device, is characterized in that:
Comprise the compression unit, drying unit, film separation unit and the cryogenic separation unit that connect successively;
Described compression unit, comprises at least one compressor connected successively, a heat exchanger and a gas-liquid separator;
Described drying unit, comprise at least two adsorption towers connected successively, described adsorption tower is built with drier;
Described film separation unit, comprises membrane separator;
Described cryogenic separation unit, comprises at least one efficient multi-channel heat exchanger, at least one low temperature gas-liquid separator, at least one gas expansion equipment and at least one expansion of liquids equipment; Described membrane separator outlet connects hot media channel C-C, the low temperature gas-liquid separator entrance of efficient multi-channel heat exchanger successively; Low temperature gas-liquid separator outlet at bottom is connecting fluid volume expansion equipment, the cold medium channel D-D of efficient multi-channel heat exchanger, pipeline k successively; Low temperature gas-liquid separator top exit connects cold medium channel A-A, the gas expansion equipment of efficient multi-channel heat exchanger successively, the cold medium channel B-B of efficient multi-channel heat exchanger, pipeline o.
2. polypropylene tail gas recovery device according to claim 1, it is characterized in that: in drying unit, described drier is selected from activated alumina, silica gel, molecular sieve.
3. polypropylene tail gas recovery device according to claim 1, is characterized in that: in film separation unit, is provided with Hydrogen Separation film in described membrane separator;
Described Hydrogen Separation film is selected from the one in the metal films such as polyimides, polysulfones, Nomex, acetate fiber, polyphenylene oxide, palladium film.
4. polypropylene tail gas recovery device according to claim 1, it is characterized in that: in cryogenic separation unit, described expansion of liquids equipment is selected from throttle expansion valve.
5. polypropylene tail gas recovery device according to claim 1, it is characterized in that: in cryogenic separation unit, described gas expansion equipment is selected from turbo-expander, air wave refrigerating device.
6. polypropylene tail gas recovery device according to claim 1, is characterized in that: in cryogenic separation unit, and described efficient multi-channel heat exchanger is selected from plate-fin heat exchanger or around heat exchange of heat pipe.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520563229.6U CN204830683U (en) | 2015-07-30 | 2015-07-30 | Polypropylene tail gas recovery unit |
| PCT/CN2015/087629 WO2017016006A1 (en) | 2015-07-30 | 2015-08-20 | Polypropylene tail gas recovery device and recovery method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520563229.6U CN204830683U (en) | 2015-07-30 | 2015-07-30 | Polypropylene tail gas recovery unit |
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| CN204830683U true CN204830683U (en) | 2015-12-02 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105004140A (en) * | 2015-07-30 | 2015-10-28 | 大连欧科膜技术工程有限公司 | Polypropylene tail gas recovery device and recovery method |
| CN106695890A (en) * | 2016-12-29 | 2017-05-24 | 成都国珈星际固态锂电科技有限公司 | Glove box system and inert gas recovery method |
| CN112857809A (en) * | 2020-12-31 | 2021-05-28 | 中国航发沈阳发动机研究所 | Low-temperature heat exchange device |
| CN114225622A (en) * | 2022-02-23 | 2022-03-25 | 北京科力丹迪技术开发有限责任公司 | Exhaust gas recovery method and device |
-
2015
- 2015-07-30 CN CN201520563229.6U patent/CN204830683U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105004140A (en) * | 2015-07-30 | 2015-10-28 | 大连欧科膜技术工程有限公司 | Polypropylene tail gas recovery device and recovery method |
| CN106695890A (en) * | 2016-12-29 | 2017-05-24 | 成都国珈星际固态锂电科技有限公司 | Glove box system and inert gas recovery method |
| CN106695890B (en) * | 2016-12-29 | 2019-11-01 | 成都国珈星际固态锂电科技有限公司 | A kind of glove box system and a kind of inert gas recovery method |
| CN112857809A (en) * | 2020-12-31 | 2021-05-28 | 中国航发沈阳发动机研究所 | Low-temperature heat exchange device |
| CN112857809B (en) * | 2020-12-31 | 2022-08-19 | 中国航发沈阳发动机研究所 | Low-temperature heat exchange device |
| CN114225622A (en) * | 2022-02-23 | 2022-03-25 | 北京科力丹迪技术开发有限责任公司 | Exhaust gas recovery method and device |
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