CN107875668A - A kind of cryogenic condensation separation method of C2 C5 alkene tail gas - Google Patents
A kind of cryogenic condensation separation method of C2 C5 alkene tail gas Download PDFInfo
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- CN107875668A CN107875668A CN201711361242.3A CN201711361242A CN107875668A CN 107875668 A CN107875668 A CN 107875668A CN 201711361242 A CN201711361242 A CN 201711361242A CN 107875668 A CN107875668 A CN 107875668A
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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
- B01D53/002—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 condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/0075—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with heat exchanging
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/009—Collecting, removing and/or treatment of the condensate
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/0093—Removing and treatment of non condensable gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
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- Separation By Low-Temperature Treatments (AREA)
Abstract
The present invention relates to a kind of cryogenic condensation separation method of C2 C5 alkene tail gas, comprise the following steps：(1) heat exchange cooling is carried out using heat exchanger to C2 C5 alkene tail gas, the gas after heat exchange cooling carries out gas-liquid separation through the first gas-liquid separator；(2) gas obtained after separating is generated electricity into expander to low pressure, expanding machine output work for generating set；(3) gas after expanding carries out gas-liquid separation through the second gas-liquid separator, qualified discharge after the C2 C5 alkene tail gas in the gas and heat exchanger discharged from the second gas-liquid separator is exchanged heat；First gas-liquid separator, the liquid olefin of the second gas-liquid separator discharge are sent into other technological processes after supercharging and recycled as raw material.System provided by the invention is particularly suitable for use in the processing of propylene in tail gas, using separation and Extraction of the present invention propylene composition therein, makes in tail gas carbohydrate content less than the exhaust emission standard that country limits.
Description
Technical field
The present invention relates to vent gas treatment field, and in particular to a kind of cryogenic condensation separation method of C2-C5 alkene tail gas, this
System is particularly suitable for use in the processing of the tail gas for preparing expoxy propane.
Background technology
According to《Discharge standard of air pollutants GB16297-1996》, except boiler, industrial furnace, thermal power plant, coking
Stove, cement plant, odorant discharge, automobile and motorcycle emission are outer, it is specified that 33 kinds of air dirts of other air pollution emissions
The emission limit of thing is contaminated, its index system is that highest allows concentration of emission, highest to allow rate of discharge and uncontrollable discharge to monitor
Concentration limit, it is 273K to give temperature, every pollution on the basis of dry air when pressure is 101325Pa under standard state
The highest limit value of thing.Discharge wherein for new pollution sources atmosphere pollution is made as defined below：
Required according to above-mentioned environmental protection standard, for containing hydro carbons (especially preparing the propylene in expoxy propane tail gas) air
The gas discharge of pollutant, by being investigated to current technology, mainly there is following two processing schemes：1 diffuses a partner burning side
Case
Gas containing hydro carbons atmosphere pollution is discharged, igniting is diffused frequently with concentration, nytron is made in torch
Thing is converted into the gas of environmental sound in high-temp combustion process, so as to reach the purpose of environmental emission standard.For this project
The tail gas with pressure containing a small amount of propylene of processing, mouth of pipe progress completely burned directly can be being diffused, propylene is fully converted to two
Carbonoxide and water are emitted into air again.However, the tail gas containing propylene of such low content, main component is nitrogen, it is entered
Row ignition bleeding generally requires burns (generally use natural gas) with the combustion-supporting companion of the gas of high heating value, realizes qualified discharge, ensures peace
Full production.The system mainly includes diffusing torch, diffuses switch board, igniter guard box, diffusion valve electric operator, holds together fire
Valve, fire valve, high-energy igniter, high pressure spot firelock, igniting private cable, flame monitoring temperature sensor etc..The technology is relative
Comparative maturity, however it is maximum the shortcomings that be, in order to convert a small amount of propylene, be filled with the burning gas of substantial amounts of high heating value,
Its energy resource consumption is huge, and economy is very poor；Further, since propylene and burning gas change into substantial amounts of CO2 emission,
Under the current situation for subtracting carbon pressure power abruptly increase, diffuse partner's burning scheme and be obviously badly in need of being substituted by other vent gas treatment schemes.
2HC absorber adsorption schemes
The key of absorption method is adsorbent and absorbing process device configuration.This method is by containing in hydrocarbon emission
Hydrocarbon molecules are adsorbed onto on adsorbent, are then again separated it from adsorbent, can reuse again after collecting and handling
In production or sell.
For a long time, people adsorb these chemical organic compounds waste gas using activated carbon granule as adsorbent always, still
Because the surface area of activated carbon granule is smaller, in order to increase activated carbon contact area, just must largely fill so that adsorbent equipment body
Product is huge, and the time one is grown, and carbon particle can become powder, influence adsorbance, and What is more, and it needs often to change, more
Black dirt rises from all around when changing, and seriously pollutes workplace.Black dirt can also enter operator's respiratory tract, endanger human health.Active carbon fibre
Dimension (hereinafter referred to as ACF) is the manufactured fibrous novel adsorption material after high temperature cabonization, activation using viscous glue based fibre as raw material
Material, compared with granular active carbon, ACF has the advantages of notable：(1) specific surface area is big, and effective adsorbance is high.(2) inhale
Fu ﹑ desorption strokes are short, speed is fast, and desorption, regeneration power consumption are low.(3) shape is variable, easy to use.(4) can produce as needed
The special ACF for the energy that has specific characteristics is provided, intensity is good, will not cause secondary pollution.
Although the hydrocarbon content in adsorbing and removing tail gas has above advantage, for preparing in expoxy propane tail gas containing a small amount of
The discharge waste gas of propylene, after adsorbent absorption propylene, it is desorbed and collected it is extremely difficult, and because tolerance is larger,
So that adsorbent device volume is huge, take up an area big, cost height, and sorbent life is shorter, is formed after solid waste still to ring
The risk of pollution be present in border.
The content of the invention
Instant invention overcomes deficiency of the prior art, it is to provide that a kind of green, energy resource consumption is small and cost
The cryogenic condensation separation method of low C2-C5 alkene tail gas.
The concrete technical scheme of the present invention is as follows：
A kind of cryogenic condensation separation method of C2-C5 alkene tail gas, comprises the following steps：
(1) heat exchange cooling is carried out using heat exchanger to C2-C5 alkene tail gas, the gas after heat exchange cooling is through the first gas-liquid point
Gas-liquid separation is carried out from device；
(2) gas obtained after separating enters expander to low pressure, expanding machine output work to be carried out for generating set
Generate electricity；
(3) gas after expanding carries out gas-liquid separation through the second gas-liquid separator, from the gas of the second gas-liquid separator discharge
Qualified discharge after body is exchanged heat with the C2-C5 alkene tail gas in heat exchanger；
First gas-liquid separator, the liquid olefin of the second gas-liquid separator discharge are sent into after supercharging in other technological processes
Recycled as raw material.
Preferably, the C2-C5 alkene tail gas is the tail gas containing propylene.
In order to further reduce the propylene content in tail gas, the propylene content in tail gas is set to be converted into liquid hydrocarbon；It is preferred that
, the cryogenic condensation separation method of the C2-C5 alkene tail gas comprises the following steps：
(1) tail gas containing propylene exchanged heat using first-class heat exchanger, exchange heat after gas enter the 3rd gas-liquid separation
Device carries out gas-liquid separation, the high boiling component of tail gas is condensed and separated in the 3rd gas-liquid separator, is arranged through liquid outlet
Go out, the gas obtained after separation exchanged heat using secondary heat exchanger, exchange heat after gas enter promoting the circulation of qi through the first gas-liquid separator
Liquid separates；
(2) gas obtained after separating enters expander to low pressure, expanding machine output work to be carried out for generating set
Generate electricity；
(3) gas after expanding carries out gas-liquid separation through the second gas-liquid separator, from the gas of the second gas-liquid separator discharge
Qualified discharge after body is exchanged heat with the tail gas containing propylene in secondary heat exchanger, first-class heat exchanger successively；First gas-liquid separation
Device, the liquid of the second gas-liquid separator discharge enter in the first vacuum insulation basin, the liquid of the first vacuum insulation basin outflow
Alkene is sent into after supercharging in other technological processes to be recycled as raw material；The processing gas of first vacuum insulation basin outflow is carried out
Torch burning processing.
Preferably, the cryogenic condensation separation method of the C2-C5 alkene tail gas, comprises the following steps：
(1) tail gas containing propylene is exchanged heat using first-class heat exchanger enters the 3rd gas-liquid to the gas after 0~5 DEG C, heat exchange
Separator carries out gas-liquid separation, the high boiling component of tail gas is condensed and separated in the 3rd gas-liquid separator, through liquid discharge
Mouth discharge, the gas obtained after separation are exchanged heat to the gas after -107.2 DEG C~-95.2 DEG C, heat exchange using secondary heat exchanger
Body carries out gas-liquid separation through the first gas-liquid separator；
(2) gas obtained after separating is used for into expander to 0.26MPa~0.34MPa, expanding machine output work
Generating set is generated electricity；
(3) gas after expanding carries out gas-liquid separation through the second gas-liquid separator, from the gas of the second gas-liquid separator discharge
Qualified discharge after body is exchanged heat with the tail gas containing propylene in secondary heat exchanger, first-class heat exchanger successively；First gas-liquid separation
Device, the liquid of the second gas-liquid separator discharge enter in the first vacuum insulation basin, the liquid of the first vacuum insulation basin outflow
Alkene is pressurized to more than 2.6Mpa through the first cryogenic pump, is preferably pressurized to after 2.6- 5MPa to be sent into other technological processes and makees
Recycled for raw material；The processing gas of first vacuum insulation basin outflow carries out torch burning processing.
When the first gas-liquid separator inlet temperature is higher than -95.2 DEG C, propylene content will be above in discharge gas
100ppm, no longer meet emission request；, will not due to the limitation of design of heat exchanger area when the temperature is less than -107.2 DEG C
Can guarantee that the normal operation of system, thus after separation obtained gas using secondary heat exchanger exchanged heat to -107.2 DEG C~-
95.2 DEG C, heat exchange after gas enter back into the first gas-liquid separator carry out gas-liquid separation.
When outlet pressure of expansion machine is higher than 0.34MPa, the normal operation of system can not be ensured, while by discharge gas
Pressure is higher than 0.15MPa limitation, and the pressure must not also be less than 0.26MPa；So gas obtained after being separated in step (2)
Generated electricity into expander to 0.26MPa~0.34MPa, expanding machine output work for generating set.
Because the C3 product populations of the second gas-liquid separator are relatively fewer, in order that the propylene in tail gas more switchs to liquid
Body olefin recovery utilizes, it is preferred that in step (3), the liquid of the first gas-liquid separator discharge enters the first vacuum insulation basin
In, the liquid of the second gas-liquid separator discharge enters in the second vacuum insulation basin, from the liquid of the second vacuum insulation basin outflow
Body is pressurized to more than 1.65Mpa through the second cryogenic pump, enters the first vacuum insulation basin after being preferably pressurized to 1.65-3Mpa
In, the liquid olefin of the first vacuum insulation basin outflow is pressurized to more than 2.6Mpa through the first cryogenic pump, is preferably pressurized to
It is sent into after 2.6-5MPa in other technological processes and is recycled as raw material；First vacuum insulation basin, the second vacuum insulation basin
The processing gas of outflow carries out torch burning processing.
In order to reduce the loss of the first vacuum insulation basin and the second vacuum insulation basin internal drop, more liquid are obtained
Body alkene, in step (3) preferably, the pressure store of the first vacuum insulation basin is 1.65-3MPa；Second vacuum insulation basin
Pressure store be 0.1-0.4MPa.
It is as follows that expanding machine output work is used for the method that generating set is generated electricity：Expanding machine output shaft and reduction box input shaft
Drive connection, reduction gearbox output shaft are connected with generator input shaft；Expanding machine output work driving generator rotates, and carries out simultaneously
Net generates electricity；Externally output electric work.
In order to effectively trap the propylene in tail gas, it is preferred that first gas-liquid separator, the second gas-liquid separation
Contain mesh mist eliminator in device, the 3rd gas-liquid separator.Because the content of propylene in tail gas is too small, it is necessary to using silk screen demisting
Device carries out gas-liquid separation, and the cryogenic gas for being entrained with vaporific lime set enters in column gas-liquid separator, the multi-layer silk screen on top
On due to collide, adsorb and surface tension effects under polymerization, lime set is captured as drop and to the bottom of gas-liquid separator
Portion assembles, and is finally collected in liquid form.
Due to liquefied propylene be mainly it is vaporific enter separator, in order to effectively trap, it is preferred that the silk screen removes
The aperture of day with fog filtering silk screen is 500-1000 mesh.
In order that the output work of gas expansion is preferably utilized, it is preferred that the expansion-pressure ratio of described expanding machine is
4.8~5.8.
Present invention is particularly suitable for the processing for the tail gas for preparing expoxy propane, the hydrocarbon content in tail gas is propylene, is used
Separation and Extraction propylene composition therein of the present invention, carbohydrate content in tail gas is set to be less than the exhaust emission standard that country limits.This hair
The bright energy that need not additionally consume other forms, also can reach the requirement of environmental emission, more will not be substantial amounts of to environmental emission
Carbon dioxide；The pressure energy of tail gas can be converted into mechanical energy additionally by expansion machinery, for driving generating set to enter
Row generates electricity；The propylene finally reclaimed will be collected with the liquid form of higher degree, can be again introduced into chemical industry stream as raw material
Journey participates in production, has considerable economy.Therefore the present invention has green, the small and economic triple advantages of energy resource consumption.
In addition, the pressure energy of propylene tail gas is converted into mechanical energy by the present invention, and for driving generating set to be generated electricity, hair
Group of motors floor space is smaller；The liquid discharged from the first gas-liquid separator, the second gas-liquid separator without carrying out gas-liquid again
Separation, is directly entered vacuum insulation basin, and can be used as raw material after the liquid olefin supercharging of vacuum insulation basin outflow is used for
In other technological processes；Technique is more easy, and cost is low.
Brief description of the drawings
Fig. 1 is the process chart of the present invention
Embodiment
The present invention is further illustrated below in conjunction with accompanying drawing.It is heat exchanger that the present invention uses, gas-liquid separator, expanding machine, true
Empty adiabatic basin, cryogenic pump etc. are all existing；So it be not described in detail.
Embodiment 1
The tail gas containing propylene is the tail gas containing propylene, and the tail gas is to prepare tail gas caused by expoxy propane.
Exhaust gas composition containing propylene：Nitrogen (92mol%), oxygen (4mol%), propylene (4mol%)；
Exhaust temperature：313K(40℃)；
Tail gas pressure：1.8MPa(pabs)；
Exhaust flow：11723kg/h(3.256kg/s,219500Nm3/h)。
Referring to Fig. 1, the direction of arrow in Fig. 1 represents gas or liquid flow direction in the present invention；A kind of tail gas containing propylene
Cryogenic condensation separation method, comprise the following steps：
(1) the tail gas 1a containing propylene is exchanged heat using first-class heat exchanger HX1 enters the to the gas 1 after 0~5 DEG C, heat exchange
Gas-liquid separation is carried out in three gas-liquid separator Sep-1, in the 3rd gas-liquid separator Sep-1, the height in the tail gas containing propylene
Boiling point component Liq-1, which is condensed, to be separated, and is discharged through liquid outlet, and the gas 2 obtained after separation is using secondary heat exchanger HX2
Exchanged heat and carry out gas-liquid separation through the first gas-liquid separator Sep-2 to the gas 3 after -107.2 DEG C~-95.2 DEG C, heat exchange；
Substantial amounts of propylene product Liq-2 is separated in the first gas-liquid separator Sep-2；
(2) gas 4 obtained after the first gas-liquid separator Sep-2 separation is expanded into expanding machine Exp-1
0.26MPa~0.34MPa, expanding machine output shaft are connected with reduction box input shaft, and reduction gearbox output shaft inputs with generator
Axle is connected；Expanding machine output work driving generator rotates, and is generated electricity by way of merging two or more grid systems, externally exports electric work；
(3) gas 5 after expanding carries out gas-liquid separation through the second gas-liquid separator Sep-3, from the second gas-liquid separator
The gas 6 of Sep-3 discharges exchanged heat with gas 2 in secondary heat exchanger HX2 successively, exchange heat after obtained gas 7 with containing
The tail gas 1a of propylene is exchanged heat in first-class heat exchanger HX1, the gas 7a qualified discharges from first-class heat exchanger HX1 out.
The propylene product Liq-2 isolated through the first gas-liquid separator Sep-2 enters the first vacuum insulation basin tank1
In, the pressure store of the first vacuum insulation basin be 1.65-3MPa, the propylene product that the second gas-liquid separator Sep-3 is isolated
Liq-3 enters in the second vacuum insulation basin tank2, the pressure store of the second vacuum insulation basin is 0.1-0.4MPa, from the
The liquid 8a of two vacuum insulation basin tank2 outflows forms liquid 8 after the second cryogenic pump pump1 is pressurized to 1.65-3Mpa,
Liquid 8 enters in the first vacuum insulation basin tank1, and the liquid olefin 9 of the first vacuum insulation basin tank1 outflows is low through first
Warm pump pump2 forms liquid 9a after being pressurized to 2.6-5MPa, and liquid 9a is sent into other technological processes to be recycled as raw material；The
Processing gas 1, the processing gas 2 of the second vacuum insulation basin tank2 outflows of one vacuum insulation basin tank1 outflows carry out fire
Torch burning is handled.
In order to effectively trap the propylene in tail gas, the first gas-liquid separator that the present invention uses, the second gas-liquid separation
Contain mesh mist eliminator in device, the 3rd gas-liquid separator, the aperture of the mesh mist eliminator filtering silk screen is 500-1000 mesh.
The expansion-pressure ratio for the expanding machine that the present invention uses is 4.8~5.8.
The Specifeca tion speeification of embodiment 1 is as shown in the table：
The basic parameter of the embodiment 1 of table 1
Present invention is particularly suitable for the processing for the tail gas for preparing expoxy propane, the hydrocarbon content in tail gas is propylene, is used
Separation and Extraction propylene composition therein of the present invention, carbohydrate content in tail gas is set to be less than the exhaust emission standard that country limits.This hair
The bright energy that need not additionally consume other forms, also can reach the requirement of environmental emission, more will not be substantial amounts of to environmental emission
Carbon dioxide；The pressure energy of tail gas can be converted into mechanical energy additionally by expansion machinery, for driving generating set to enter
Row generates electricity；The propylene finally reclaimed will be collected with the liquid form of higher degree, can be again introduced into chemical industry stream as raw material
Journey participates in production, has considerable economy.Therefore the present invention has green, the small and economic triple advantages of energy resource consumption.
Claims (10)
1. a kind of cryogenic condensation separation method of C2-C5 alkene tail gas, it is characterised in that comprise the following steps：
(1) heat exchange cooling is carried out using heat exchanger to C2-C5 alkene tail gas, the gas after heat exchange cooling is through the first gas-liquid separator
Carry out gas-liquid separation；
(2) gas obtained after separating is generated electricity into expander to low pressure, expanding machine output work for generating set；
(3) expand after gas through the second gas-liquid separator carry out gas-liquid separation, from the second gas-liquid separator discharge gas with
Qualified discharge after C2-C5 alkene tail gas in heat exchanger is exchanged heat；
First gas-liquid separator, the liquid olefin of the second gas-liquid separator discharge are sent into conduct in other technological processes after supercharging
Raw material recycles.
2. according to the method for claim 1, it is characterised in that the C2-C5 alkene tail gas is the tail gas containing propylene.
3. according to the method for claim 2, it is characterised in that comprise the following steps：
(1) tail gas containing propylene exchanged heat using first-class heat exchanger, exchange heat after gas enter into the 3rd gas-liquid separator
Row gas-liquid separation, the high boiling component of tail gas is condensed and separated in the 3rd gas-liquid separator, is discharged through liquid outlet, point
The gas obtained from after exchanged heat using secondary heat exchanger, exchange heat after gas carry out gas-liquid point through the first gas-liquid separator
From；
(2) gas obtained after separating is generated electricity into expander to low pressure, expanding machine output work for generating set；
(3) expand after gas through the second gas-liquid separator carry out gas-liquid separation, from the second gas-liquid separator discharge gas according to
Qualified discharge after the tail gas containing propylene is exchanged heat in secondary and secondary heat exchanger, first-class heat exchanger；First gas-liquid separator,
The liquid of two gas-liquid separators discharge enters in the first vacuum insulation basin, the liquid olefin warp of the first vacuum insulation basin outflow
It is sent into after supercharging in other technological processes and is recycled as raw material；The processing gas of first vacuum insulation basin outflow carries out torch combustion
Burning processing.
4. according to the method for claim 3, it is characterised in that comprise the following steps：
(1) tail gas containing propylene is exchanged heat using first-class heat exchanger enters the 3rd gas-liquid separation to the gas after 0~5 DEG C, heat exchange
Device carries out gas-liquid separation, the high boiling component of tail gas is condensed and separated in the 3rd gas-liquid separator, is arranged through liquid outlet
Go out, the gas obtained after separation is exchanged heat to the gas after -107.2 DEG C~-95.2 DEG C, heat exchange through the using secondary heat exchanger
One gas-liquid separator carries out gas-liquid separation；
(2) gas obtained after separating enters expander to 0.26MPa~0.34MPa, and expanding machine output work is used to generate electricity
Unit is generated electricity；
(3) expand after gas through the second gas-liquid separator carry out gas-liquid separation, from the second gas-liquid separator discharge gas according to
Qualified discharge after the tail gas containing propylene is exchanged heat in secondary and secondary heat exchanger, first-class heat exchanger；First gas-liquid separator,
The liquid of two gas-liquid separators discharge enters in the first vacuum insulation basin, the liquid olefin warp of the first vacuum insulation basin outflow
First cryogenic pump is sent into other technological processes as raw material recycling after being pressurized to 2.6-5MPa；First vacuum insulation basin stream
The processing gas gone out carries out torch burning processing.
5. according to the method for claim 4, it is characterised in that in step (3), the liquid of the first gas-liquid separator discharge enters
Enter in the first vacuum insulation basin, the liquid of the second gas-liquid separator discharge enters in the second vacuum insulation basin, true from second
The liquid of empty adiabatic basin outflow enters in the first vacuum insulation basin after the second cryogenic pump is pressurized to 1.65-3MPa, and first
The liquid olefin of vacuum insulation basin outflow is sent into conduct in other technological processes after the first cryogenic pump is pressurized to 2.6-5MPa
Raw material recycles；First vacuum insulation basin, the processing gas of the second vacuum insulation basin outflow carry out torch burning processing.
6. according to the method for claim 5, it is characterised in that in step (3), the pressure store of the first vacuum insulation basin
For 1.65-3MPa；The pressure store of second vacuum insulation basin is 0.1-0.4MPa.
7. the method according to claim 3 to 6, it is characterised in that expanding machine output work is used for what generating set was generated electricity
Method is as follows：Expanding machine output shaft is connected with reduction box input shaft, and reduction gearbox output shaft connects with the transmission of generator input shaft
Connect；Expanding machine output work driving generator rotates, and is generated electricity by way of merging two or more grid systems；Externally output electric work.
8. according to the method described in any one of claim 3 to 6, it is characterised in that first gas-liquid separator, the second gas-liquid
Contain mesh mist eliminator in separator, the 3rd gas-liquid separator.
9. according to the method for claim 8, it is characterised in that the aperture of the mesh mist eliminator filtering silk screen is 500-
1000 mesh.
10. according to the method described in any one of claim 3 to 6, it is characterised in that the expansion-pressure ratio of described expanding machine is 4.8
~5.8.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109157939A (en) * | 2018-10-22 | 2019-01-08 | 上海灿越化工科技有限公司 | Cooling-the eddy flow that gasifies coalesces combined type gas-liquid separator and its application |
| CN110368772A (en) * | 2019-01-31 | 2019-10-25 | 滨化集团股份有限公司 | The processing method and its device of tail gas during a kind of propylene oxide, dichloropropane loading-unloading vehicle |
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