CN106000017A - Recovery method and recovery device for polyethylene technical tail gas through vapor phase method - Google Patents
Recovery method and recovery device for polyethylene technical tail gas through vapor phase method Download PDFInfo
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- CN106000017A CN106000017A CN201610500701.0A CN201610500701A CN106000017A CN 106000017 A CN106000017 A CN 106000017A CN 201610500701 A CN201610500701 A CN 201610500701A CN 106000017 A CN106000017 A CN 106000017A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
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Abstract
The invention provides a recovery method and a recovery device for polyethylene technical tail gas through a vapor phase method. The recovery method comprises the following steps: S1) firstly compressing and cooling the tail gas and then performing organic vapor membrane separation, thereby acquiring a first gas and a second gas; S2) performing hydrogen membrane separation on the first gas, thereby acquiring hydrogen and a third gas; S3) introducing the third gas into a deep cold separating unit, firstly condensing ethylene and then sending to the upstream position, recovering the cooling rapacity of the separated nitrogen and then discharging to a pipeline of a flare system or pressurizing through a nitrogen compressor and returning to a polymerization unit of polyethylene device for conveying or purging and purifying the powder products; S4) introducing a second gas component into the device for secondary compressing and cooling, thereby returning the acquired liquid to the polymerization unit of polyethylene device and performing polymerization reaction again, returning the non-condensed gas to the front end of the compressor and performing compressing separation again. According to the technical scheme provided by the invention, the recovery rate of the valued hydrocarbon matters is increased.
Description
Technical field
The present invention relates to chemical field, in particular to recovery method and the recovery dress of a kind of gas-phase polyethylene process tail gas
Put.
Background technology
Gas-phase polyethylene production technology in process of production, in order to maintain the stable of each component of reactor and discharges material, needs
The a large amount of rich hydrocarbon tail gas of discharge.
At present, the solvent recovery technology from vent gas of gas-phase polyethylene production technology mainly has two kinds, and one is tail gas through multi-stage compression and cold
Solidifying, condensed liquid is back to response system, it is impossible to the gas major part discharge torch of condensation, partial gas returns and is used for
Purge gas；Another kind of recovery process is basically identical with the first, is to set up a set of organic steam membrance separation system in fixed gas rear end
System, the small part hydrocarbon gas in fixed gas can be recycled to the compressibility of front end, but cause simultaneously and do not coagulate by this film separation system
The pressure of gas declines, and the utilization rate of fixed gas reduces, and compared with the first recovery process, only slightly improves valuable hydrocarbon
The recovery ratio of matter.
The at present recycling of tail gas has the disadvantage in that 1) each component of tail gas can not fully recycle, and has valency in a large number
Value gas enters flare system, causes waste；2) can not make full use of compression energy to reclaim, the power causing compressor is big,
Power consumption is high, and cost recovery is high.
Summary of the invention
It is desirable to provide the recovery method of a kind of gas-phase polyethylene process tail gas and retracting device, to improve valuable time
Receive.
To achieve these goals, according to an aspect of the invention, it is provided the recovery of a kind of gas-phase polyethylene process tail gas
Method.The method comprises the following steps: S1, and gas-phase polyethylene process tail gas carries out organic steam film after one stage of compression cools down
Separate, obtain the first gas rich in ethylene, nitrogen and hydrogen and containing rich in organic second gas of carbon more than two；S2, the
One gas carries out hydrogen membrane separation, obtains hydrogen and the 3rd gas；S3, the 3rd gas enters into cryogenic separation unit, and ethylene is first
First being condensed, deliver to upstream device after cold is reclaimed in heat exchange, the nitrogen separated, after cold recovery, is emitted into fire
The pipeline of torch system or be back to polyethylene device polymerized unit by nitrogen compressor supercharging and carry for powder product or powder produces
The purging of product purifies；And S4, the second gas component enters two-stage compression cooling, the liquid obtained is back to polyethylene device
Polymerized unit participates in polyreaction again, it is impossible to the gas of enough condensations is back to the front end of compressor and is again compressed separating.
Further, gas-phase polyethylene process tail gas initially entered the first surge tank before carrying out one stage of compression cooling and delays
Punching；After one stage of compression cools down, enter the second surge tank buffer；The second gas obtained after organic steam membrance separation
Initially enter after the 3rd surge tank buffers and carry out two-stage compression cooling again.
Further, one stage of compression cooling and two-stage compression cooling are to be realized by the compression cylinder being sequentially connected in series and heat exchanger.
Further, the hydrogen separated delivers to fuel gas pipe network.
Further, cryogenic separation unit is unpowered cryogenic separation unit.
Further, in S3, ethylene is after after being condensed, the remaining gas rich in nitrogen flows through Turbine expansion unit, by pressure energy
It is converted into cold with cooling ethylene and nitrogen.
According to a further aspect in the invention, it is provided that the retracting device of a kind of gas-phase polyethylene process tail gas.This retracting device bag
Include: one stage of compression cooling unit, be connected with gas-phase polyethylene process tail gas discharge pipe line；Organic steam film separation unit,
Be provided be connected with one stage of compression cooling unit air inlet, for discharging the first gas rich in ethylene, nitrogen and hydrogen
First gas outlet and for discharging rich in the second gas outlet of organic second gas of carbon more than two；Hydrogen membrane separative element,
It is provided with air inlet, hydrogen outlet and the 3rd gas outlet that the first gas outlet with organic steam film separation unit is connected；
Cryogenic separation unit, is connected with the 3rd gas outlet of hydrogen membrane separative element, is used for isolating ethylene and nitrogen, is provided with
Ethylene outlet and nitrogen outlet, nitrogen outlet is provided with and is emitted into the pipeline of flare system or will return polyethylene dress after nitrogen supercharging
Put the polymerized unit the first return line for the purging purification of the conveying of powder product or powder product；And two-stage compression cooling is single
Unit, is connected with the second gas outlet of organic steam film separation unit, is provided with and liquid is back to polyethylene device polymerization list
Unit again participates in the second return line of polyreaction and is back to one stage of compression cooling unit front end with the gas that will not be able to condensation
3rd return line.
Further, one stage of compression cooling unit upstream is provided with into the first surge tank, one stage of compression cooling unit and organic steam
It is provided with the second surge tank between film separation unit, between organic steam film separation unit and two-stage compression cooling unit, is provided with
Three surge tanks.
Further, one stage of compression cooling unit includes one stage of compression cylinder and the first-class heat exchanger being sequentially connected in series；Two-stage compression is cold
But unit includes two-stage compression cylinder and the secondary heat exchanger being sequentially connected in series.
Further, the hydrogen outlet of hydrogen membrane separative element communicates with fuel gas pipe network.
Further, cryogenic separation unit is unpowered cryogenic separation unit.
Further, this retracting device also includes: Turbine expansion unit, is connected with cryogenic separation unit, is used for will be enriched in nitrogen
The pressure of the gas of gas can be converted into cold with cooling ethylene and nitrogen.
Application technical scheme, by optimizing whole recovery process flow process, uses organic steam membrane separation process and deep cooling
Separating technology, improves the recovery ratio of the valuable hydrocarbons such as ethylene, heavy hydrocarbons (carbon more than two component)；Additionally, enter
One step comprehensive utilization compression energy, reduces energy consumption, reduction cost recovery in hydrocarbons removal process in discharge gas.
Accompanying drawing explanation
The Figure of description of the part constituting the application is used for providing a further understanding of the present invention, and the present invention's is schematic real
Execute example and illustrate for explaining the present invention, being not intended that inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 shows the schematic flow sheet of the recovery method of the gas-phase polyethylene process tail gas of according to embodiments of the present invention 1.
Detailed description of the invention
It should be noted that in the case of not conflicting, the embodiment in the application and the feature in embodiment can be mutually combined.
Describe the present invention below with reference to the accompanying drawings and in conjunction with the embodiments in detail.
According to a kind of typical embodiment of the present invention, it is provided that the recovery method of a kind of gas-phase polyethylene process tail gas.This recovery
Method comprises the following steps: S1, and gas-phase polyethylene process tail gas carries out organic steam membrance separation after one stage of compression cools down,
To the first gas rich in ethylene, nitrogen and hydrogen with containing rich in organic second gas of carbon more than two；S2, the first gas enters
Row hydrogen membrane separates, and obtains hydrogen and the 3rd gas；S3, the 3rd gas enters into cryogenic separation unit, and first ethylene be condensed
Getting off, deliver to upstream device after cold is reclaimed in heat exchange, the nitrogen separated, after cold recovery, is emitted into flare system
Pipeline or by nitrogen compressor supercharging be back to polyethylene device polymerized unit for powder product carry or the purging of powder product
Purify；And S4, the second gas component enters two-stage compression cooling, the liquid obtained is back to polyethylene device polymerized unit
Again participate in polyreaction, it is impossible to the gas of enough condensations is back to the front end of compressor and is again compressed separating.
Wherein, upstream device refers to the device that again carbon two component can be purified and be separated, for example, it is possible to be separation of olefins
Device etc..
Application technical scheme, by optimizing whole recovery process flow process, uses organic steam membrane separation process and deep cooling
Separating technology, improves the recovery ratio of the valuable hydrocarbons such as ethylene, heavy hydrocarbons (carbon more than two component)；Additionally, enter
One step comprehensive utilization compression energy, reduces energy consumption, reduction cost recovery in hydrocarbons removal process in discharge gas.Wherein, ethylene
The response rate improve, mainly by deep cooling process for separating, gaseous ethylene can be condensed into liquid, and reclaim；Heavy hydrocarbons (carbon
More than two components) the response rate improve, mainly by recycling cold energy, the gas temperature of compressor secondary exit port is down to
Lower, so that more heavy hydrocarbon component condensation, and it is back to polyethylene device polymerized unit by pump.Preferably, gas phase
Method polyethylene process tail gas initially entered the first surge tank before carrying out one stage of compression cooling and buffers；Cold through one stage of compression
But enter the second surge tank after to buffer；The second gas obtained after organic steam membrance separation initially enters the 3rd surge tank
Two-stage compression cooling is carried out again after buffering.Using surge tank, the gas pressure on the one hand reducing inter-stage fluctuates, on the other hand,
Gas can be remained in surge tank, in order to avoid impacting compressor due to the liquid occurred after compression cooling.
According to a kind of typical embodiment of the present invention, one stage of compression cooling and two-stage compression cooling are the compressions by being sequentially connected in series
Cylinder and heat exchanger realize.
According to a kind of typical embodiment of the present invention, the hydrogen separated delivers to fuel gas pipe network, naturally it is also possible to he uses.
Preferably, cryogenic separation unit is unpowered cryogenic separation unit.
According to a kind of typical embodiment of the present invention, in S3, ethylene after being condensed the remaining gas rich in nitrogen flow through turbine
After expanding unit, pressure can be converted into cold, in order to cool down ethylene and nitrogen.
According to a kind of typical embodiment of the present invention, it is provided that the retracting device of a kind of gas-phase polyethylene process tail gas.This recovery
Device includes: one stage of compression cooling unit, is connected with gas-phase polyethylene process tail gas discharge pipe line；Organic steam membrance separation
Unit, be provided be connected with one stage of compression cooling unit air inlet, for discharge rich in the first of ethylene, nitrogen and hydrogen
First gas outlet of gas and for discharging the second gas outlet rich in organic second gas of carbon more than two；Hydrogen membrane is divided
From unit, it is provided with air inlet, hydrogen outlet and the 3rd gas that the first gas outlet with organic steam film separation unit is connected
Body exports；Cryogenic separation unit, is connected with the 3rd gas outlet of hydrogen membrane separative element, is used for isolating ethylene and nitrogen,
Being provided with ethylene outlet and nitrogen outlet, nitrogen outlet is provided with and is emitted into the pipeline of flare system or poly-by returning after nitrogen supercharging
Ethylene unit polymerized unit is for the first return line of the purging purification of the conveying of powder product or powder product；Two-stage compression cools down
Unit, is connected with the second gas outlet of organic steam film separation unit, is provided with and liquid is back to polyethylene device polymerization
Unit is again participated in the second return line of polyreaction and is back to one stage of compression cooling unit front end with the gas that will not be able to condensation
The 3rd return line.
Application technical scheme, by optimizing whole recovery process flow process, uses organic steam membrane separation process and deep cooling
Separating technology, improves the recovery ratio of the valuable hydrocarbons such as ethylene, heavy hydrocarbons (carbon more than two component)；Additionally, enter
One step comprehensive utilization compression energy, reduces energy consumption, reduction cost recovery in hydrocarbons removal process in discharge gas.Wherein, ethylene
The response rate improve, mainly by deep cooling process for separating, gaseous ethylene can be condensed into liquid, and reclaim；Heavy hydrocarbons (carbon
More than two components) the response rate improve, mainly by recycling cold energy, the gas temperature of compressor secondary exit port is down to
Lower, so that more heavy hydrocarbon component condensation, and it is back to polyethylene device polymerized unit by pump.
Preferably, one stage of compression cooling unit upstream is provided with into the first surge tank, one stage of compression cooling unit and organic steam film
It is provided with the second surge tank between separative element, between organic steam film separation unit and two-stage compression cooling unit, is provided with the 3rd
Surge tank.Using surge tank, the gas pressure on the one hand reducing inter-stage fluctuates, on the other hand, and can be cold due to compression by gas
The liquid occurred the most afterwards remains in surge tank, in order to avoid impacting compressor.
According to a kind of typical embodiment of the present invention, one stage of compression cooling unit includes the one stage of compression cylinder and being sequentially connected in series
Level heat exchanger；Two-stage compression cooling unit includes two-stage compression cylinder and the secondary heat exchanger being sequentially connected in series.
According to a kind of typical embodiment of the present invention, the hydrogen outlet of hydrogen membrane separative element communicates with fuel gas pipe network.
Preferably, cryogenic separation unit is unpowered cryogenic separation unit.
According to a kind of typical embodiment of the present invention, this device farther includes: Turbine expansion unit, with cryogenic separation unit
Being connected, the pressure of the gas for will be enriched in nitrogen can be converted into cold with cooling ethylene and nitrogen.
Beneficial effects of the present invention is further illustrated below in conjunction with embodiment.
Embodiment 1
Idiographic flow and scheme are as follows:
As shown in Figure 1:
S1, the tail gas in gas-phase polyethylene production process, after the first surge tank 11 buffering, enters the one stage of compression being sequentially connected in series
Cylinder 211 and first-class heat exchanger 212 carry out one stage of compression cooling, enter into the second surge tank 12 and buffer, subsequently into having
Machine steam blanket separative element 30 separates, and obtains the first gas rich in ethylene, nitrogen and hydrogen and containing having rich in carbon more than two
Second gas of machine thing；
S2, the first gas enters hydrogen membrane separative element 40 and carries out hydrogen membrane separation, obtains hydrogen and the 3rd gas, and hydrogen is delivered to
Fuel gas pipe network；
S3, the 3rd gas enters into unpowered cryogenic separation unit 50, and (wherein, unpowered cryogenic separation unit 50 connects second
Knockout drum 52), owing to the dew point temperature of ethylene is far above nitrogen, first ethylene be condensed, after cold is reclaimed in heat exchange
Delivering to upstream device, pressure after after being condensed, the remaining gas rich in nitrogen flows through Turbine expansion unit 51, can be converted by ethylene
For cold with cooling ethylene and nitrogen；The nitrogen separated, after cold recovery, is emitted into the pipeline of flare system or by nitrogen
Return polyethylene device polymerized unit after supercharging and purify for the purging of the conveying of powder product or powder product；And
S4, the second gas enters into the 3rd surge tank 13 and buffers, subsequently into two-stage compression cylinder 221 He being sequentially connected in series
Secondary heat exchanger 222 carries out two-stage compression cooling, and after the first knockout drum 223 separates, the liquid obtained is back to poly-second
Alkene device polymerized unit participates in polyreaction again, and on-condensible gas is back to the first surge tank 11.
In the present embodiment, the ethylene separated and nitrogen carry out heat exchange again with chilled water, improve the organic efficiency of cold energy；
Chilled water after cooling is contained in freezing water pot 60, as the cooling medium of heat exchanger.
As can be seen from the above description, the above embodiments of the present invention achieve following technique effect:
1) tail gas i.e. carries out membrance separation, by ethylene, ethane, nitrogen, hydrogen etc. and carbon more than two group after entering one section of compression
Separate, reduce two-stage nitration compression power consumption.
2) tail gas is after separating-purifying, is obtained for recycling, decreases CO2Discharge Deng waste gas.
3) by the cold recovery of gas after refrigeration, maximally utilized compression energy, reduced the unit consumption of exhaust gas recovery system.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for those skilled in the art
For, the present invention can have various modifications and variations.All within the spirit and principles in the present invention, any amendment of being made, etc.
With replacement, improvement etc., should be included within the scope of the present invention.
Claims (12)
1. the recovery method of a gas-phase polyethylene process tail gas, it is characterised in that comprise the following steps:
S1, described gas-phase polyethylene process tail gas through one stage of compression cool down after carry out organic steam membrance separation, obtain rich in
First gas of ethylene, nitrogen and hydrogen and containing rich in organic second gas of carbon more than two；
S2, described first gas carries out hydrogen membrane separation, obtains hydrogen and the 3rd gas；
S3, described 3rd gas enters into cryogenic separation unit, and first ethylene be condensed, after cold is reclaimed in heat exchange
Delivering to upstream device, the nitrogen separated, after cold recovery, is emitted into the pipeline of flare system or passes through nitrogen compressor
Supercharging is back to polyethylene device polymerized unit and purifies for the purging of the conveying of powder product or powder product；And
S4, described second gas enters two-stage compression cooling, the liquid obtained is back to the polymerization of described polyethylene device single
Unit participates in polyreaction again, it is impossible to the gas of enough condensations is back to the front end of compressor and is again compressed separating.
Recovery method the most according to claim 1, it is characterised in that described gas-phase polyethylene process tail gas carry out described
Initially enter the first surge tank before one stage of compression cooling to buffer；Second is entered after described one stage of compression cools down
Surge tank buffers；Described second gas obtained after described organic steam membrance separation initially enters the 3rd surge tank and enters
Two-stage compression cooling is carried out again after row buffering.
Recovery method the most according to claim 1, it is characterised in that the cooling of described one stage of compression and described two-stage compression cool down
It is the compression cylinder by being sequentially connected in series and heat exchanger realization.
Recovery method the most according to claim 1, it is characterised in that the hydrogen separated delivers to fuel gas pipe network.
Recovery method the most according to claim 1, it is characterised in that described cryogenic separation unit is unpowered cryogenic separation list
Unit.
Recovery method the most according to claim 1, it is characterised in that in described S3, ethylene is remaining rich in nitrogen after being condensed
After the gas of gas flows through Turbine expansion unit, pressure can be converted into cold with cooling ethylene and nitrogen.
7. the retracting device of a gas-phase polyethylene process tail gas, it is characterised in that including:
One stage of compression cooling unit, is connected with gas-phase polyethylene process tail gas discharge pipe line；
Organic steam film separation unit, be provided be connected with described one stage of compression cooling unit air inlet, for discharging
Rich in ethylene, nitrogen and hydrogen the first gas the first gas outlet and for discharging rich in carbon more than two organic the
Second gas outlet of two gases；
Hydrogen membrane separative element, is provided with the air inlet that the first gas outlet with described organic steam film separation unit is connected
Mouth, hydrogen outlet and the 3rd gas outlet；
Cryogenic separation unit, is connected with the 3rd gas outlet of described hydrogen membrane separative element, be used for isolating ethylene and
Nitrogen, is provided with ethylene outlet and nitrogen outlet, and described nitrogen outlet is provided with and is emitted into the pipeline of flare system or by nitrogen
The first return for the purging purification of the conveying of powder product or powder product of the polyethylene device polymerized unit is returned after gas supercharging
Pipeline；And
Two-stage compression cooling unit, is connected with the second gas outlet of described organic steam film separation unit, be provided with by
Liquid is back to polyethylene device polymerized unit and again participates in the second return line of polyreaction and will not be able to the gas of condensation
Body is back to the 3rd return line of described one stage of compression cooling unit front end.
Retracting device the most according to claim 7, it is characterised in that described one stage of compression cooling unit upstream is provided with into
One surge tank, is provided with the second surge tank between described one stage of compression cooling unit and described organic steam film separation unit,
It is provided with the 3rd surge tank between described organic steam film separation unit and described two-stage compression cooling unit.
Retracting device the most according to claim 7, it is characterised in that described one stage of compression cooling unit includes being sequentially connected in series
One stage of compression cylinder and first-class heat exchanger；Described two-stage compression cooling unit includes the two-stage compression cylinder and two being sequentially connected in series
Level heat exchanger.
Retracting device the most according to claim 7, it is characterised in that the hydrogen outlet of described hydrogen membrane separative element and fuel
Gas pipe network communicates.
11. retracting devices according to claim 7, it is characterised in that described cryogenic separation unit is unpowered cryogenic separation list
Unit.
12. retracting devices according to claim 7, it is characterised in that farther include:
Turbine expansion unit, is connected with described cryogenic separation unit, and the pressure of the gas for will be enriched in nitrogen can convert
For cold with cooling ethylene and nitrogen.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610500701.0A CN106000017A (en) | 2016-06-29 | 2016-06-29 | Recovery method and recovery device for polyethylene technical tail gas through vapor phase method |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201610500701.0A CN106000017A (en) | 2016-06-29 | 2016-06-29 | Recovery method and recovery device for polyethylene technical tail gas through vapor phase method |
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Cited By (6)
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| CN106397090A (en) * | 2016-12-07 | 2017-02-15 | 北京华福工程有限公司 | Gas stripping concentration and separation method and gas stripping concentration and separation equipment for ethylene crude product gas prepared through acetylene hydrogenation |
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| CN106731441A (en) * | 2016-12-07 | 2017-05-31 | 杭州欧缘科技有限公司 | A kind of system and method for being used for effluent gas recovery in olefin polymer production |
| CN112023605A (en) * | 2019-06-03 | 2020-12-04 | 中石化南京化工研究院有限公司 | Organic steam retrieves experimental apparatus |
| CN112169549A (en) * | 2020-10-15 | 2021-01-05 | 大连理工大学盘锦产业技术研究院 | Method for recovering tail gas of gas phase polyethylene device |
| CN114471090A (en) * | 2022-02-07 | 2022-05-13 | 大连理工大学 | Membrane coupling separation process for comprehensively utilizing ethylene device flare gas |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106397090A (en) * | 2016-12-07 | 2017-02-15 | 北京华福工程有限公司 | Gas stripping concentration and separation method and gas stripping concentration and separation equipment for ethylene crude product gas prepared through acetylene hydrogenation |
| CN106731441A (en) * | 2016-12-07 | 2017-05-31 | 杭州欧缘科技有限公司 | A kind of system and method for being used for effluent gas recovery in olefin polymer production |
| CN106731441B (en) * | 2016-12-07 | 2023-01-24 | 杭州欧缘科技有限公司 | System and method for vent gas recovery in olefin polymer production |
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| CN112023605A (en) * | 2019-06-03 | 2020-12-04 | 中石化南京化工研究院有限公司 | Organic steam retrieves experimental apparatus |
| CN112169549A (en) * | 2020-10-15 | 2021-01-05 | 大连理工大学盘锦产业技术研究院 | Method for recovering tail gas of gas phase polyethylene device |
| CN114471090A (en) * | 2022-02-07 | 2022-05-13 | 大连理工大学 | Membrane coupling separation process for comprehensively utilizing ethylene device flare gas |
| CN114471090B (en) * | 2022-02-07 | 2022-10-04 | 大连理工大学 | Membrane coupling separation process for comprehensively utilizing ethylene device torch gas |
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Application publication date: 20161012 |