CN208186972U - A kind of device of olefin hydrocarbon apparatus recycling discharge gas - Google Patents
A kind of device of olefin hydrocarbon apparatus recycling discharge gas Download PDFInfo
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- CN208186972U CN208186972U CN201721323848.3U CN201721323848U CN208186972U CN 208186972 U CN208186972 U CN 208186972U CN 201721323848 U CN201721323848 U CN 201721323848U CN 208186972 U CN208186972 U CN 208186972U
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Abstract
The utility model discloses the devices that a kind of olefin hydrocarbon apparatus recycles discharge gas, and device mainly includes the equipment such as heat exchanger, knockout drum and turbo-expander.Methane column overhead discharge gas enters recyclable device progress cryogenic separation in the discharge gas and olefin separation of polyethylene device, cooling capacity needed for the on-condensible gas expansion cooling isolated by knockout drum provides cooling, the liquid rich in high-carbon hydrocarbon are sent into polyethylene device as unstripped gas.The liquid phase isolated can reenter methane column overhead as rectifying liquid in methane column overhead discharge gas, and what gas phase was separated with the discharge gas of polyethylene device, which be rich in low-carbon appropriate hydrocarbon gas, converges and send to olefin separation.The present apparatus without exterior power input, using discharge gas pressure expansion cooling provide gas liquefaction separate institute's chilling requirement, realize discharge gas all of, have good realistic meaning and application value.
Description
Technical field
The utility model belongs to the field of resource recovery technique that chemical industry tail gas overbottom pressure utilizes and extracts useful component, tool
Body is a kind of device of olefin hydrocarbon apparatus recycling discharge gas.
Background technique
Each polyolefin device can generate the discharge gas with reaction mass in process of production, and discharge gas enters respectively existing
Recovery system recycles most non-methane hydrocarbon component (ethylene, propylene, third through the modes such as overcompression/condensation or pressure-variable adsorption
C2~the C6 such as alkane component), the consumption of the raw materials such as monomer, comonomer and condensing agent is reduced to the maximum extent.Due to by existing
The restriction of equipment cannot all condense out the components such as all ethylene, 1- butylene, isopentane, therefore in the tail of discharge torch
Contain many hydrocarbon components and nitrogen in gas, causes the waste of raw material, would seriously pollute the environment simultaneously, be unable to reach regulation
Discharge index.
Compression condensation method is a kind of traditional gas separating method, and process is simple, treating capacity is big, is returned in polyolefin discharge gas
It has been widely used in receipts.As much as possible to recycle hydro carbons, first discharge gas is pressurizeed by compressor to improve discharge gas
Dew point, then by HP cooler and high pressure condenser cooling condensation, gas-liquid mixture enters high pressure lime set tank and carries out gas-liquid point
From the condensate liquid isolated uses pumped back reaction system together with low pressure condensate liquid, and discharge tail-gas a part is defeated as powder
It supplies gas, extra is discharged into torch.But this method is not suitable for the situation that coercibility hydro carbons concentration is lower in discharge gas, compression condensation
Method low efficiency, recovery efficiency is not high, can not recycle inert gas, degassing is not achieved in inert gas concentration in uncooled discharge gas
Concentration requirement, flare system can only be discharged, cause to waste.Compression condensation method has the hydro carbons of C4 and bigger carbon number biggish time
Yield, but the limitation due to being under pressure with condensation temperature, to the more difficult recycling of the hydro carbons of C1~C3, generally no greater than 30%.
Patent US 5,521,264, which is disclosed, a kind of utilizes monomer in Physical Absorption-analytic method recycling polyolefin discharge gas
Method, process flow are as follows: discharge gas recycles condensate liquid by compression condensation technique, and uncooled discharge gas enters absorption tower；?
Absorb the hydro carbons in discharge gas with absorbent in absorption tower, obtain the overhead gas stream containing nitrogen, light component, and containing absorbent and
It is absorbed the tower bottom liquid stream of monomer, the optional discharge torch of overhead gas stream as conveying gas or removes degassing cabin, and tower bottom liquid stream enters
Desorber；By the absorbent and monomer separation in tower bottom liquid stream in desorber, obtain the tower top stream stock containing monomer and contain to absorb
The tower bottom stream stock of agent, tower bottom stream stock return to absorption tower and are recycled, reaction monomers Returning reacting system.
Patent US 5,681,908 increases the separation and recovery process of byproduct of reaction on this basis.Absorption-desorption method
Although hydro carbons can further be recycled on the basis of compression condensation method, equipment investment is big, and process is complicated, and it is low to absorb needs
Warm condition, desorption need hot conditions, are required to additional energy consumption and public work, and operating cost is high.
Gaseous jet simulation method also can be used in effluent gas recovery, and it is raw that patent 200920203363.X discloses a kind of polypropylene
Propylene recovery unit during production, the tail gas being discharged in production process is through dust filter unit, buffer gas tank, compressor, condenser
After obtain gas-liquid mixture, gas-liquid mixture is sent into gas-liquid separator and carries out gas-liquid separation, and on-condensible gas is by filtering and heat tracing
Enter membrane separator afterwards, the hydrocarbon components such as propylene permeate lateral enrichment in film, return to the entrance of compressor.Patent uses compression condensation
Method in conjunction with UF membrane makes propylene recovery rate be increased to 99%, however the membrane separation device used in patent is only by hydro carbons point
From without separating small-molecule substance with inert gas, therefore the infiltration residual air obtained after UF membrane cannot recycle, and make
At the wasting of resources, increase production cost.
Patent CN102389643A discloses the method for effluent gas recovery in a kind of production of olefin polymer, polyolefin resin
The discharge gas obtained after resin devolatilization after compression condensation process enter gas-liquid separation process isolate condensed fluid with it is not cold
Solidifying gas；Condensed fluid is divided into two strands after degassing process isolates inert gas and lower carbon number hydrocarbons, one returns to compression condensation
Process, another strand of Returning reacting system；Uncondensed gas isolates hydrocarbon component by gas separation process and returns to compression condensation
Process, while small-molecule substance discharge flare system is isolated, as resin transfer gas, remaining returns to resin devolatilization for tail gas part
Process.But this process needs to increase discharge atmospheric pressure, increases UF membrane in uncondensed gas gas separation process
Device, so that equipment investment increases, since UF membrane needs to work in normal temperature state, the cooling capacity of uncondensed gas gas is not
It can be fully used.
It can be seen that there are recovery efficiencies is not high, it is low effectively to recycle for effluent gas recovery technique in the production of existing alkene
Boiling point hydro carbons can not recycle inert gas, the deficiencies of equipment investment is big, energy consumption is high, therefore, invent a kind of simple and effective recycling and arrange
Deflation each component, recovery method and device without additionally increasing power consumption have great economic interests and realistic meaning.
Utility model content
The purpose of the utility model is to overcome the deficiencies in the prior art, provide a kind of dress of olefin hydrocarbon apparatus recycling discharge gas
It sets.
The purpose of this utility model is to provide the device that a kind of olefin hydrocarbon apparatus recycles discharge gas, which mentions without the external world
For power, using the pressure throttling cooling of discharge gas itself as the cooling capacity of gas liquefaction separation is provided, extremely by discharge air cooling
Low temperature, and effective component is separated and recovered in knockout drum, tail gas pressure energy is made full use of, product yield is increased, is dropped
Low production cost, while reducing exhaust emissions, protect environment.
The purpose of this utility model is achieved through the following technical solutions:
A kind of device of olefin hydrocarbon apparatus recycling discharge gas, including first-class heat exchanger E1, knockout drum V1, secondary heat exchanger
E2, knockout drum V2 and V3, turbo-expander TU1 and TU2.
Main flow technique:
Polyethylene device discharges gas after first-class heat exchanger E1 and secondary heat exchanger E2 cooling, arranges in gas-liquid two-phase
It deflates and enters knockout drum V2 separation, the condensed gas rich in hydro carbons is after tank bottom return two heat exchangers offer cooling capacity, rewarming
It forms gas-liquid two-phase and enters knockout drum V1, after the condensate liquid rich in high-carbon hydrocarbon is from tank bottom extraction into first-class heat exchanger rewarming
It is sent into polyolefin device, is produced after low-boiling low-carbon hydrocarbon gasification from abhiseca.Knockout drum V2 abhiseca uncondensed gas is height
The inert gas of purity provides cold into after turbo-expander TU2 expansion cooling into secondary heat exchanger and first-class heat exchanger
It measures, the regeneration gas that can be used as drying device after rewarming uses.
The discharge gas of olefin separation methane column overhead by first-class heat exchanger E1 and secondary heat exchanger E2 cooling after,
Enter knockout drum V3 separation in gas-liquid two-phase discharge gas, condensed gas returns to heat exchanger from tank bottom and provides cooling capacity, rewarming
The rectifying of methane column overhead is returned afterwards to provide after uncondensed gas enters turbo-expander TU2 expansion cooling into secondary heat exchanger
Cooling capacity, then the lower carbon number hydrocarbons gas phase with knockout drum V1 abhiseca converges feeding olefin separation, as olefin separation
Unstripped gas.
The heat exchanger uses plate-fin heat exchanger or wound tube heat exchanger, preferably plate-fin heat exchanger.
The gas-liquid separation device is knockout drum, deflector type gas-liquid separator, silk screen gas-liquid separator, centrifugal gas
Liquid/gas separator or spiral board gas-liquid separator, preferably knockout drum.
The pressure energy for discharging gas is converted cooling capacity required for cryogenic separation by the turbo-expander, can use gas
Body bearing turbo-expander, oil bearing turbo-expander or scroll expander can be reasonably selected according to processing tolerance size.
Condensate liquid liquid described in main flow technique rich in high-carbon hydrocarbon is mainly C4+, and quality adds up to polyethylene dress
90~95% of C4+ constituent mass score in discharge gas are set, i.e. C4+ component recovery can reach 90~95% or more.
Knockout drum V1 abhiseca uncondensed gas described in main flow technique is mainly N2 and C2,
C2 constituent mass is that polyethylene device discharges 40% of C2 constituent mass score in gas.Knockout drum V2 abhiseca
Uncondensed gas is that the inert gas of high-purity is mainly N2, and N2 purity can reach 95% or more, can be used as drying device again
Anger uses.
Condensed fluid in knockout drum V3 described in main flow technique is mainly C3 and C3+, and the rate of recovery can arrive
To 95% or more.Uncondensed gas in knockout drum V3 is mainly C2 and N2, with gas-liquid described in main flow technique point
It is similar from tank V1 abhiseca uncondensed gas component, it can converge to and be sent together to olefin separation as unstripped gas.
The workflow of utility model device is as follows:
Polyethylene device discharge gas is cooled to -110~-115 DEG C by first-class heat exchanger E1 and secondary heat exchanger E2, is in
Gas-liquid two-phase discharge gas enters knockout drum V2 separation, and the condensed gas rich in hydro carbons produces from tank bottom, is back to second level and changes
Hot device heat exchange provides cooling capacity, forms gas-liquid two-phase after extremely -50~-65 DEG C of rewarming, into knockout drum V1, is rich in high-carbon hydrocarbon
The condensate liquid of (predominantly C4+ hydro carbons) is sent into polyolefin device after entering first-class heat exchanger rewarming from tank bottom extraction, low-boiling
It is produced after low-carbon hydrocarbon gasification from abhiseca, main component is ethylene and nitrogen.Knockout drum V2 abhiseca uncondensed gas is high-purity
The inert gas (N2 of 95~97.5% purity) of degree, expands into turbo-expander TU2, and pressure is down to from 1.25MPa
0.4MPa, greenhouse cooling return to secondary heat exchanger and first-class heat exchanger provide cooling capacity, can be used as after rewarming to -130~-140 DEG C
The regeneration gas of drying device uses.
The discharge gas of olefin separation methane column overhead is cooled to by first-class heat exchanger E1 and secondary heat exchanger E2-
105~-110 DEG C, enter knockout drum V3 separation in gas-liquid two-phase discharge gas, (main component is C3+ hydrocarbon to condensed gas
Class) secondary heat exchanger to be sent back to from tank bottom extraction that cooling capacity is provided, rewarming to -40~-45 DEG C of first is sent to methane column overhead rectifying, not
Condensed gas (main component is ethylene and nitrogen) enters turbo-expander TU2 and expands, and pressure is down to 0.4MPa from 2.65MPa,
Greenhouse cooling provides cooling capacity to -135~-142 DEG C, into secondary heat exchanger, then with the lower carbon number hydrocarbons of knockout drum V1 abhiseca
Gas phase converges feeding olefin separation, the unstripped gas as olefin separation.
Other olefin polymetiation process and Olefin Separation Technology, which generate discharge gas with pressure, can be used dress disclosed by the utility model
It sets and is recycled, the utility model is particularly suitable for gas-phase process production ethylene and polypropylene plant.
The effluent gas recovery device of the utility model has the advantage that
1) it is inputted without exterior power, the pressure expansion using discharge gas cools down, cooling capacity needed for providing cryogenic separation；
2) hydrocarbon component is separated and recovered by cryogenic gas, improves hydrocarbon recovery；
3) higher by the purity inert gas after gas fractionation unit, the regeneration gas that can be used as drying unit uses.
4) hydro carbons after separation and inert gas can enter other devices and use, after processing without pernicious gas
Discharge.
5) a whole set of effluent gas recovery device process is simple, and process unit is simple and compact, and device integrally takes up an area and invests less；
Detailed description of the invention
Fig. 1 process flow diagram.
E1- first-class heat exchanger, E2- secondary heat exchanger, V1- knockout drum, V2- knockout drum, V3- gas-liquid separation
Tank, TU1- turbo-expander, TU2- turbo-expander.
Specific embodiment
Embodiment 1
Using olefin hydrocarbon apparatus effluent gas recovery device recycle polyethylene device shown in FIG. 1 and separation of olefins
Device methane column overhead discharges gas, and it is 1.25MPa, each group shunt volume that polyethylene device, which discharges atmospheric pressure, are as follows:
Ethylene 96kg/h, nitrogen 1580kg/h, normal butane 203kg/h, iso-butane 111kg/h, isopentane 101kg/h.Alkene
It is 2.64MPa, each group shunt volume that hydrocarbon separator methane column overhead, which discharges atmospheric pressure, are as follows:
Ethylene 165kg/h, nitrogen 189kg/h, propane 558kg/h, methane 1179kg/h, propylene 45kg/h.
Predominantly C3+ hydro carbons, the flow 837.7kg/h of knockout drum V3 tower bottom extraction can be sent after recovered device
To methane column overhead rectifying, predominantly C4+, the flow 469.8kg/h of the extraction of knockout drum V1 tower bottom can send to polyethylene and fill
It sets as unstripped gas, nitrogen gas concn is 97.3% in knockout drum V2 top gas phase, flow 1610kg/h, be can be used as after rewarming
Drying device regeneration gas.
The rate of recovery after discharging the recovered system of gas hydrocarbon component are as follows: ethylene 99.9%, isopentane 99.9%, 1- hexene
99.9%, nitrogen 100%, discharge gas is fully used.
Claims (1)
1. a kind of device of olefin hydrocarbon apparatus recycling discharge gas, which is characterized in that including sequentially connected first-class heat exchanger (E1), gas
Liquid knockout drum (V1), secondary heat exchanger (E2), knockout drum (V2) and knockout drum (V3), turbo-expander (TU1) and
(TU2)；
The first-class heat exchanger and secondary heat exchanger are all made of plate-fin heat exchanger or wound tube heat exchanger；
Baffle plate, wire mesh demister and spiral board are successively installed inside the knockout drum；
The turbo-expander is using one in gas-bearing expansion turbine, oil bearing turbo-expander, scroll expander
Kind.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201721323848.3U CN208186972U (en) | 2017-10-13 | 2017-10-13 | A kind of device of olefin hydrocarbon apparatus recycling discharge gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721323848.3U CN208186972U (en) | 2017-10-13 | 2017-10-13 | A kind of device of olefin hydrocarbon apparatus recycling discharge gas |
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| CN208186972U true CN208186972U (en) | 2018-12-04 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109942365A (en) * | 2019-04-22 | 2019-06-28 | 中科瑞奥能源科技股份有限公司 | The recovery process and device of alkene alkane or hydrocarbon mixture |
| CN109999529A (en) * | 2019-04-22 | 2019-07-12 | 中科瑞奥能源科技股份有限公司 | Chemical industry tail gas process for separating and recovering and device |
-
2017
- 2017-10-13 CN CN201721323848.3U patent/CN208186972U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109942365A (en) * | 2019-04-22 | 2019-06-28 | 中科瑞奥能源科技股份有限公司 | The recovery process and device of alkene alkane or hydrocarbon mixture |
| CN109999529A (en) * | 2019-04-22 | 2019-07-12 | 中科瑞奥能源科技股份有限公司 | Chemical industry tail gas process for separating and recovering and device |
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