CN105080278A - Oil and gas recovery method - Google Patents
Oil and gas recovery method Download PDFInfo
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- CN105080278A CN105080278A CN201510496054.6A CN201510496054A CN105080278A CN 105080278 A CN105080278 A CN 105080278A CN 201510496054 A CN201510496054 A CN 201510496054A CN 105080278 A CN105080278 A CN 105080278A
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- 238000000034 method Methods 0.000 title claims abstract description 63
- 238000011084 recovery Methods 0.000 title claims abstract description 27
- 238000001179 sorption measurement Methods 0.000 claims abstract description 60
- 230000003197 catalytic effect Effects 0.000 claims abstract description 43
- 230000003647 oxidation Effects 0.000 claims abstract description 42
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 42
- 238000009833 condensation Methods 0.000 claims abstract description 30
- 230000005494 condensation Effects 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 239000002699 waste material Substances 0.000 claims abstract description 12
- 239000000919 ceramic Substances 0.000 claims abstract description 7
- 238000003795 desorption Methods 0.000 claims abstract description 5
- 238000010521 absorption reaction Methods 0.000 claims description 19
- 239000003054 catalyst Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- 239000003595 mist Substances 0.000 claims description 3
- 238000003032 molecular docking Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 238000005057 refrigeration Methods 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 78
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 26
- 230000009102 absorption Effects 0.000 description 17
- 239000003921 oil Substances 0.000 description 12
- 239000003610 charcoal Substances 0.000 description 11
- 238000007084 catalytic combustion reaction Methods 0.000 description 6
- 150000001555 benzenes Chemical class 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- -1 benzene hydrocarbon Chemical class 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 206010020852 Hypertonia Diseases 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000003421 catalytic decomposition reaction Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Natural products C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000000700 radioactive tracer Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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- Separation Of Gases By Adsorption (AREA)
Abstract
The invention relates to an oil and gas recovery method. The oil and gas recovery method mainly solves the problems that in the prior art, emission on standard cannot be achieved, and energy consumption is high. According to the oil and gas recovery method, an adsorption system, a desorption system, a condensation system and a low-temperature catalytic oxidation system are included. A tail gas raw material pipeline is connected with all adsorption tank tail gas inlet pipelines. An adsorption tank tail gas outlet pipeline is connected with the low-temperature catalytic oxidation system. An adsorption tank desorption outlet pipeline is connected with inlets of two screw vacuum units. Outlets of the screw vacuum units are connected with the condensation system. The condensation system comprises a condensing unit precooling system and a multilevel refrigeration heat exchanger. An outlet of the condensation system is connected with a waste liquid tank and an inlet of the low-temperature catalytic oxidation system. The low-temperature catalytic oxidation system comprises a heater, a low-temperature accelerant bed, a high-temperature accelerant bed and a heat pipe ceramic heat exchanger. The technical scheme that an outlet of the low-temperature catalytic oxidation system is connected with a chimney well solves the above problems, and the oil and gas recovery method can be used for tail gas treatment.
Description
Technical field
The present invention relates to a kind of oil-gas recovery method.
Background technology
Gasoline, benzene class and boat coal are in shipment process, a large amount of organic gas can be produced, not only cause energy waste, and contaminated environment, therefore will recycle this kind of gas, along with the regulation of national standard is more and more stricter, traditional simple process combination can not meet harsh requirement, therefore invent one " circulation absorption+condensation+low-temperature catalytic oxidation " oil-gas recovery method, NMHC can be met lower than 120mg/m
3, benzene is lower than 2mg/m
3.Mention crude oil shipment oil-gas recovery method in patent 201310234691.7, its main technological route is " two-step desulfurization system+two-stage absorption+low temperature absorption ", and do not embody low-temperature catalytic oxidation, export targets is difficult to meet benzene lower than 2mg/m
3if want to meet above index, then need increasing energy consumption.Patent 201320584179.0 mentions a kind of harbour device for recovering oil and gas, and it only adopts the method for cryogenic condensation, compared with this patent, has discharge index high, the feature that energy consumption is large.Patent 201420384177.1 mentions a kind of harbour sour crude oil gas recovery processing system, its technology path is " desulfurization+two-stage absorption+compression condensation+fuel recovery ", and it is directly discharged by charcoal canister, is only applicable to the occasion of process NMHC, if process benzene class steam, cannot be up to standard
The present invention solves this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is cannot qualified discharge, problem that energy consumption is higher in prior art, provides a kind of new oil-gas recovery method.The method is used in vent gas treatment, has qualified discharge, advantage that energy consumption is lower.
For solving the problem, the technical solution used in the present invention is as follows: a kind of oil-gas recovery method, adopt the oil gas in device for recovering oil and gas recovery terminal ship process, described device for recovering oil and gas comprises adsorption system, desorption system, condenser system and low-temperature catalytic oxidation system, described adsorption system comprises four adsorption tanks, tail gas feed line is connected with each adsorption tanks gas inlet pipeline, adsorption tanks offgas outlet pipeline is connected with low-temperature catalytic oxidation system, adsorption tanks desorb outlet line is connected with two screw vacuum unit inlet, screw vacuum machine set outlet is connected with condenser system, described condenser system comprises condensation unit chilldown system, multi-stage refrigerating heat exchanger, and condenser system outlet is connected with waste liquid tank, low-temperature catalytic oxidation system entry respectively, described low-temperature catalytic oxidation system comprises heater, low temperature catalyst bed, high temperature catalyst bed, heat pipe ceramic heat exchanger, and low-temperature catalytic oxidation system outlet is connected with chimney, in terminal ship process, the gas of volatilization, by ship bank docking system, is incorporated into device for recovering tail gas by blower fan, every bar vapor delivery line is equipped with the rotating speed that micro-pressure sensor controls blower fan, adsorption tanks are built with active carbon, and organic gas is absorbed by active carbon, and the gas after filtration enters low-temperature catalytic oxidation system, is processed further, and gas up to standard directly discharges, when some adsorption tanks absorption is saturated, two vacuum pump set start simultaneously, and the organic gas after desorb enters condenser system and carries out condensation, and the liquid of condensation enters waste liquid tank and reclaims, and the gas be not condensed enters low-temperature catalytic oxidation system, first tail gas after absorption and the gas be not condensed enter the pretreatment system of low-temperature catalytic oxidation, mist is diluted to less than 25% of LEL, by the effect of air-introduced machine, be introduced into the heating clamber of heater, and by heat pipe ceramic heat exchanger with carry out heat exchange through the gas of high-temperature S removal process before, gas after heat exchange is transformed by two-stage catalytic oxidation bed, and gas up to standard after treatment enters air through chimney.
In technique scheme, preferably, described tail gas feed line is provided with surge tank.
In technique scheme, preferably, be connected with oil pump inlet after described adsorption tanks offgas outlet pipeline is connected with condenser system outlet line, fuel pump outlet is connected with low-temperature catalytic oxidation system.
In technique scheme, preferably, described vacuum pump set adopts VFC, and the circulating water cooling system that the cooling of vacuum pump set is provided by cooling tower supplies.
In technique scheme, preferably, described condenser system comprises three tier structure cold heat exchanger.
In technique scheme, preferably, described four adsorption tanks are in parallel.
In technique scheme, preferably, described tail gas feed line is connected with chimney entrance.
The oil-gas recovery method that the present invention relates to, for reclaiming oil gas, the benzene class steam and the organic gas such as coal steam that navigate that produce in many terminal ships process.The process route adopted is: many adsorption tanks circulation absorption, two vavuum pump desorb, multi-stage mechanical condensation, low-temperature catalytic oxidation.In terminal ship process, the gas of volatilization, by ship bank docking system, is incorporated into device for recovering tail gas by blower fan, every bar vapor delivery line is equipped with the rotating speed that micro-pressure sensor controls blower fan, prevents cabin pressure from changing too greatly.
Adsorption system comprises four charcoal canisters, 12 electrically operated valves, four magnetic valves and corresponding measuring instrument etc.Vacuum desorption system comprises two cover screw vacuum units, circulating cooling system etc.Multi-stage mechanical condenser system comprises compressor, expansion valve, air-cooled condenser, oil gas condensation special evaporator, oil eliminator etc., and is double evaporators structure.Low-temperature catalytic oxidation system comprises pretreatment system, high/low temperature catalyst bed, thermal storage ceramic, heat exchanger, on-line analysis instrument etc.
Charcoal canister is built with active carbon, and organic gas is absorbed by charcoal canister, and the gas after filtration enters low-temperature catalytic oxidation system, is processed further, and gas up to standard directly discharges.Four charcoal canister circulation absorptions, in parallel use, when one of them is when adsorbing, and other three or in desorb, or in wait, the advantage recycling canister organic gas desorb to be got off in a short period of time, and desorb is very thorough.Being used alternatingly of charcoal canister is realized by the opening and closing of corresponding electrically operated valve.When some charcoal canister absorption is saturated, two vacuum pump set start simultaneously, organic gas after desorb enters multi-stage condensing device and carries out condensation, according to the difference of each material freezing point, being condensed into liquid respectively, returning waste liquid tank and reclaim, being solidified for preventing the liquid of discharging, waste liquid tank is warmed to above zero, delivers to outside device.Low-temperature catalytic oxidation system is entered together with the gas that a small amount of gas be not condensed and charcoal canister are discharged, process, first the pretreatment system of low-temperature catalytic oxidation is entered, mist is diluted to less than 25% of LEL, by the effect of air-introduced machine, be introduced into heating clamber, and by heat exchange ware with carry out heat exchange through the gas of high-temperature S removal process before.Gas after heat exchange is transformed by two-stage catalytic oxidation bed, and gas up to standard after treatment enters air.Vacuum pump set adopts VFC, prevents that initial start stage air quantity is excessive to be impacted charcoal bed and condensation unit.The circulating water cooling system that the cooling of vacuum pump set is provided by cooling tower supplies.Owing to containing benzene in recover materials, electric tracing and isothermal holding to be carried out to package unit.
This patent provides the oil-gas recovery method of a kind of " circulation absorption+condensation+low-temperature catalytic oxidation ", can process the different organic gas volatilized when many harbours are loaded onto ship simultaneously, meet up-to-date national standard and Industry code requirements, NMHC≤120mg/m
3, clearance>=97%, benzene≤2mg/m
3, and energy consumption is lower, achieves good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of device of the present invention.
1-blower fan A; 2-micro-pressure sensor A; 3-electrically operated valve A; 4-blower fan B; 5-micro-pressure sensor B; 6-electrically operated valve B; 7-blower fan C; 8-micro-pressure sensor C; 9-electrically operated valve C; 10-surge tank; 11-adsorption tanks A; 12-adsorption tanks B; 13-adsorption tanks C; 14-adsorption tanks D; 15-adsorption tanks A magnetic valve; 16-adsorption tanks B magnetic valve; 17-adsorption tanks C magnetic valve; 18-adsorption tanks D magnetic valve; 19-adsorption tanks A atmospheric valve; 20-adsorption tanks B atmospheric valve; 21-adsorption tanks C atmospheric valve; 22-adsorption tanks D atmospheric valve; 23-adsorption tanks A intake valve; 24-adsorption tanks B intake valve; 25-adsorption tanks C intake valve; 26-adsorption tanks D intake valve; 27-adsorption tanks A regeneration valve; 28-adsorption tanks B regeneration valve; 29-adsorption tanks C regeneration valve; 30-adsorption tanks D regeneration valve; 31-transfer valve; 32-vacuum pump set A; 33-vacuum pump set B; 34-condensation unit chilldown system; 35-one-level is freezed; 36-secondary freezes; 37-three tier structure is cold; 38-liquid level gauge; 39-waste liquid tank; 40-oil pump; 41-air-introduced machine; The online concentration meter of 42-; 43-inlet temperature meter; 44-heater; 45-low temperature catalyst bed; 46-high temperature catalyst bed; 47-heat pipe ceramic heat exchanger; 48-chimney.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Detailed description of the invention
[embodiment 1]
As shown in Figure 1, adopt " circulation absorption+condensation+low-temperature catalytic oxidation " provided by the invention oil-gas recovery method, device for recovering oil and gas is made up of four charcoal canisters, two vacuum pump set, multi-stage condensing unit, low-temperature catalytic oxidation device, surge tank, waste liquid tank and correlate meter valves etc.
The organic gas that each terminal ship produces enters oil-gas recovery method respectively by blower fan A, blower fan B, blower fan C through tail gas feed line, regulated the rotating speed of each blower fan by micro-pressure sensor A, micro-pressure sensor B, micro-pressure sensor C, prevent cabin hypertonia or too low.Electrically operated valve A, electrically operated valve B, electrically operated valve C can prevent mutual flushing between different material.The open and close of electrically operated valve are subject to the control of blower fan start stop signal.
Organic gas is first by surge tank 10, a small amount of condenses is got off and is entered surge tank, and organic gas enters adsorption tanks A, and intake valve 23 is opened, atmospheric valve 19 is opened, all the other valve closings, after adsorption tanks A absorption is saturated, start vacuum pump set 32 simultaneously, vacuum pump set 33, carry out vacuum action to adsorption tanks A, now electrically operated valve 23, electrically operated valve 19 are closed, and electrically operated valve 27 is opened.Simultaneously the electrically operated valve 24 of adsorption tanks B, electrically operated valve 20 are opened, and gas enters adsorption tanks B and adsorbs.The high concentration organic gas temperature that adsorption tanks A is got off by vacuum pump set desorb is more than 80 DEG C, be introduced into condensation unit chilldown system 34, by the recirculated water of condensation unit chilldown system, gas is dropped to normal temperature, regenerate latter stage, open magnetic valve 15, introduce nitrogen and purge charcoal bed, be beneficial to desorb thorough.High from vacuum pump set gas concentration out, temperature is high, be unfavorable for the steady operation of condensation unit, therefore first by recirculated water, gas temperature is dropped to normal temperature, gas through precooling enters one-level refrigeration, the temperature of one-level refrigeration is at about 5 DEG C, three benzene hydrocarbon gases and steam are condensed, remaining gas enters secondary refrigeration, the temperature of secondary refrigeration is about-40 DEG C, triphen class is substantially all condensed, most hydro carbons is also condensed, finally enter three tier structure cold, minimumly condense to-75 DEG C, after multi-stage condensing, major part is organic to be condensed, liquid temporarily enters waste liquid tank 39 and is stored, waste liquid tank 39 there is far transmission level meter 38, can gauging level, when arriving certain yield, tank field is returned through oil pump 40.Condensation unit adopts double evaporators structural design, prevents the situation of solidifying frost, affects package unit and normally run.
After the gas and vapor permeation that adsorption tanks light concentration gas out and condensation unit are not condensed, low-temperature catalytic oxidation system is introduced by air-introduced machine 41, it adopts the mode of low temperature catalyst, ignition temperature is less than 300 DEG C, the air quantity of air-introduced machine is controlled by the temperature of inlet temperature meter 43, heating clamber 44 is established in catalytic oxidation system, start heater, enter inner loop, when hot gas source reaches catalytic combustion temperature requirement, low-temperature catalyzed catalyst 45 and high-temperature catalytic catalyst 46 pairs of organic substances carry out catalytic decomposition, give off energy simultaneously.The heat energy of catalytic combustion can carry out heat exchange through heat-exchange device 47 to the waste gas entered, now heater quits work completely, and organic exhaust gas is in the indoor maintenance spontaneous combustion of catalytic combustion, and circulation is carried out, do not reach when requiring until stop machine catalytic combustion temperature next time, heater is opened again.Online concentration analyzer 42 for monitoring supplied materials gas concentration, catalytic oxidation front reaction concentration and outlet concentration, direct emission gases when chimney 48 is mainly used in emission compliance gas and plant failure.
Within the time of setting, adsorption tanks A desorb is complete, and adsorption tanks B absorption is simultaneously saturated, and electrically operated valve automatically switches, organic gas enters adsorption tanks C and adsorbs, and adsorption tanks B regenerates, and adsorption tanks C adsorbs saturated, regenerate, gas enters adsorption tanks D, and so forth.
Which adsorption tanks is system can enter according to the amount intelligent decision organic gas of loading onto ship simultaneously, starts several vacuum pump set.When temperature is lower than 15 degree, for preventing benzene class to condense in system blocking, starting electric tracer heating system and device is incubated.
The organic steam mean concentration volatilized in terminal ship process is generally 20%VOL, and mass concentration is about 600g/m
3, the non-methane hydrocarbon emission concentration≤80mg/m after device process
3, benzene concentration of emission≤2mg/m
3the treatment effeciency of device for recovering tail gas is 99.9%, according to the regulation of the GB31571-2015 " petro chemical industry pollutant emission standard " of up-to-date promulgation, and Air Pollutant Emission limit value, removal efficiency>=97% of NMHC in other organic exhaust gas, the discharge value≤4mg/m of benzene
3.If do not increase low-temperature catalytic oxidation device, reach above-mentioned discharge index, energy consumption needs increase by more than 50%.
[comparative example]
Existing patented technology, if the combined method only adopting absorption method, condensation method, absorption process or a few person, shortcoming is that the energy consumption of condensation method is very large, and want the requirement reaching new national standard, energy consumption at least increases by more than 50%; If oil gas is discharged in air by absorption method and goes, benzene is difficult to reach 4mg/m
3emission limit; The method of existing catalytic combustion, the requirement of GB can be reached, but because the temperature of catalytic combustion is higher, certain potential safety hazard can be brought, this patent adds low-temperature catalytic oxidation method in previous process flow process, control maximum temperature and be no more than 400 DEG C, and prime condensation method power can be reduced to and is used alone 1/2 of condensation method.
Obviously, the oil-gas recovery method of " circulation absorption+condensation+low-temperature catalytic oxidation " that this patent provides, the different organic gas volatilized when many harbours are loaded onto ship simultaneously can be processed, meet up-to-date national standard and Industry code requirements, NMHC≤120mg/m
3, clearance>=97%, benzene≤2mg/m
3, and energy consumption is lower, achieves good technique effect.
Claims (7)
1. an oil-gas recovery method, adopt the oil gas in device for recovering oil and gas recovery terminal ship process, described device for recovering oil and gas comprises adsorption system, desorption system, condenser system and low-temperature catalytic oxidation system, described adsorption system comprises four adsorption tanks, tail gas feed line is connected with each adsorption tanks gas inlet pipeline, adsorption tanks offgas outlet pipeline is connected with low-temperature catalytic oxidation system, adsorption tanks desorb outlet line is connected with two screw vacuum unit inlet, and screw vacuum machine set outlet is connected with condenser system; Described condenser system comprises condensation unit chilldown system, multi-stage refrigerating heat exchanger, and condenser system outlet is connected with waste liquid tank, low-temperature catalytic oxidation system entry respectively; Described low-temperature catalytic oxidation system comprises heater, low temperature catalyst bed, high temperature catalyst bed, heat pipe ceramic heat exchanger, and low-temperature catalytic oxidation system outlet is connected with chimney; In terminal ship process, the gas of volatilization, by ship bank docking system, is incorporated into device for recovering tail gas by blower fan, every bar vapor delivery line is equipped with the rotating speed that micro-pressure sensor controls blower fan; Adsorption tanks are built with active carbon, and organic gas is absorbed by active carbon, and the gas after filtration enters low-temperature catalytic oxidation system, is processed further, and gas up to standard directly discharges; When some adsorption tanks absorption is saturated, two vacuum pump set start simultaneously, and the organic gas after desorb enters condenser system and carries out condensation, and the liquid of condensation enters waste liquid tank and reclaims, and the gas be not condensed enters low-temperature catalytic oxidation system; First tail gas after absorption and the gas be not condensed enter the pretreatment system of low-temperature catalytic oxidation, mist is diluted to less than 25% of LEL, by the effect of air-introduced machine, be introduced into the heating clamber of heater, and by heat pipe ceramic heat exchanger with carry out heat exchange through the gas of high-temperature S removal process before, gas after heat exchange is transformed by two-stage catalytic oxidation bed, and gas up to standard after treatment enters air through chimney.
2. oil-gas recovery method according to claim 1, is characterized in that described tail gas feed line is provided with surge tank.
3. oil-gas recovery method according to claim 1, it is characterized in that described adsorption tanks offgas outlet pipeline is connected with oil pump inlet after being connected with condenser system outlet line, fuel pump outlet is connected with low-temperature catalytic oxidation system.
4. oil-gas recovery method according to claim 1, is characterized in that described vacuum pump set adopts VFC, the circulating water cooling system supply that the cooling of vacuum pump set is provided by cooling tower.
5. oil-gas recovery method according to claim 1, is characterized in that described condenser system comprises three tier structure cold heat exchanger.
6. oil-gas recovery method according to claim 1, is characterized in that described four adsorption tanks are in parallel.
7. oil-gas recovery method according to claim 1, is characterized in that described tail gas feed line is connected with chimney entrance.
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| CN105617826A (en) * | 2016-02-17 | 2016-06-01 | 大连举扬科技股份有限公司 | Low-temperature plasma oil gas ultra-clean emission treatment process and device |
| CN107297141A (en) * | 2016-04-15 | 2017-10-27 | 中国石油化工股份有限公司 | A kind of oil gas recovery treatment process and complete set of equipment |
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| CN107754546A (en) * | 2017-11-21 | 2018-03-06 | 南京都乐制冷设备有限公司 | A kind of condensation catalytic unit and processing method for handling high-concentration organic waste gas |
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