CN1366021A - Process and apparatus for recovering hydrocarbons from hydrocarbon and air mixed gas - Google Patents
Process and apparatus for recovering hydrocarbons from hydrocarbon and air mixed gas Download PDFInfo
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- CN1366021A CN1366021A CN 01100559 CN01100559A CN1366021A CN 1366021 A CN1366021 A CN 1366021A CN 01100559 CN01100559 CN 01100559 CN 01100559 A CN01100559 A CN 01100559A CN 1366021 A CN1366021 A CN 1366021A
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Abstract
A process for recovering hydrocarbons from the mixed gas of hydrocarbons and air includes such steps as pre-cooling at 0-10 deg.C, primary gas-liquid separation to separate out liquid phase, deeply cooling the gas phase at -10- -70 deg.C, and gas-liquid separation to recover liquid-state hydrocarbons. Both separators use ultrafilters.
Description
The present invention relates to a kind of method and device that reclaims hydro carbons from hydro carbons and Air mixing gas, tool this locality is said, the present invention relates to a kind of method and device that is used in combination the recovery hydro carbons of ultra-filtration technique and condensation technology.
In petroleum refining process, especially in the storage and transport process of oil product, the rate of loss of its light-end products accounts for 0.35% of crude oil processing.Along with requirement on environmental protection is improved day by day, enterprise also progressively carries out the work that oil vapour pollution is administered in recent years.But because facility does not match, the all swivel links of oil product are many, mediation technology falls behind, the not high many reasons of production management level, cause depleted uncontrollable discharge amount bigger, the state of the art of administering is also lower, makes that gas containing hydrocarbon emission control aspect is in relatively backward level on the whole in China oil storage and transportation system, compares the also bigger gap of existence with industrially developed country in the world.Again because light-end products such as gasoline product belong to the evaporable flammable and explosive substance, and has the oil gas property built up, with the easy gas cloud that forms behind the air formation explosive mixture, and along with air-flow flies away everywhere, sink to building up among depression or pipe trench at last, running into naked light after reaching finite concentration promptly can initiation fire or accident such as blast, be the security incident hidden danger in the production process, it also is the basic reason of security incident, in case, will cause the heavy losses of lives and properties toward contact in great serious accidents such as place's presence of fire of the loading and unloading oils station or blasts.At present, along with the raising of environmental protection requirement consciousness, and the successful Application of multinomial technology such as breathing roof tank, people concentrate on the emission concentration that utilizes oil gas recovery technology control oil gas to more attention in recent years, have developed dissimilar retrieving arrangements.
U.S. Pat 4,039,306 disclose a kind of from hydrocarbon gas and air mixture, reclaim hydrocarbon gas from steam stripped circulation adsorption unit.This device comprises two adsorption towers that sorbent material is housed, its automatically controlled valve feeds an adsorption tower with gas mixture, and another adsorption tower is linked to each other with stripper plant, certainly also has a kind of test set, whether the air-flow of adsorption tower needs to switch so that determine automatically to flow through, and switches if desired then to drive self-acting valve and finish this switching.Stripper plant has a vacuum pump, and its suction casing alternately links to each other with two adsorption towers and it is found time, and the gas of extraction is delivered to condensing tower again and carried out hydro carbons condensation recovery.The hydro carbons that condensation is got off removes basin, handles and the uncooled gas that gets off enters the activated adsorption tower with hydrocarbon gas and AIR MIXTURES.This invention has been used in combination adsorption technology and condensation recovery technology.
European patent EP 298288 discloses a kind of method that reduces the hydro carbons discharging by the cooling gas mixture, it adopts two clean-up stage, the part hydrocarbon emissions is cooled and settles down in first clean-up stage, the hydrocarbon emissions that will still be retained in gaseous mixture in second clean-up stage is utilized the refrigerating unit in energy drives first clean-up stage that discharges at combustion in IC engine.Gaseous mixture can carry out partly degassed at hydrocarbon compound in mass transfer rig in first clean-up stage.In addition, first clean-up stage also can contain the turbulent pipe device, to promote the further sedimentation of hydro carbons of condensation.
European patent EP 528320 discloses a kind of low temperature and has reclaimed C
2Or the technology of higher hydrocarbon more, this technology comprises: (a) gaseous stream is carried out partial condensation; (b) gaseous stream of partial condensation is separated, is separated into gaseous state component and liquid component in phase separator; (c) with condensation at low temperature the gaseous state component in (b) is carried out rectifying, produce the gaseous stream of lighter hydrocarbons and the liquid stream of heavy hydrocarbon; (d) will carry out stripping in stripping tower from the liquid component of (b) with from the heavy liquid stream of (c), the tower base stream of stripping tower is a heavier hydrocarbon products; (e) refrigerating capacity of technology mainly from adopt mixed cooling medium, one way gas recompression rerigerator.This method advantage is: owing under lower pressure, handle gaseous stream, thereby it is lower to separate required energy, and also because of adopting single compressor, equipment is also comparatively cheap.
US 5,154, then use in 735 solid adsorbent bed to reclaim hydrocarbon; 628336 of EP use gac to make vapor and reclaim hydrocarbon.
In fact will reclaim the hydro carbons in the mixed gas on a large scale, general be unableing to do without carried out the technology that condensation is reclaimed to gas, reclaims even adopt sorbent material to need that also hydro carbons is carried out final condensation.Yet headachy problem is exactly that moisture cools down from gas and becomes ice and bring one to be that trouble is as stopping up for follow-up rerigerator operation in the condensation process.In addition, the temperature of condensation is low more, and power consumption is also just big more.How to save energy consumption and also be a major issue when reclaiming hydro carbons in the gas.
Purpose of the present invention just provides a kind of method and device that reclaims hydro carbons from hydro carbons and Air mixing gas, and it not only can remove the moisture in the gaseous mixture under comparatively high temps, thereby eliminates the influence of freezing refrigerating system being brought; And can under higher relatively temperature, condensation reclaim hydro carbons, thereby reduce energy consumption.
The method that reclaims hydro carbons from hydro carbons and Air mixing gas provided by the present invention mainly comprises:
(a) hydro carbons and Air mixing gas are carried out precooling, the temperature of precooling is controlled at above zero, below 10 ℃;
(b) mixed gas after the precooling in (a) is carried out elementary gas-liquid separation, isolate wherein formed liquid phase composition;
(c) gas composition through gained after the elementary gas-liquid separation in (b) is carried out the deep cooling condensation, condensing temperature is controlled at-10 ℃～-70 ℃, reclaims the liquid hydrocarbon that wherein forms.
In addition, after the deep cooling condensation of step (c), can adopt the secondary gas-liquid separation, reclaim wherein formed liquid hydrocarbon.
In above-mentioned method, the main purpose that hydro carbons and Air mixing gas carry out the elementary gas-liquid separation of pre-cold-peace is to remove most moisture in the gas mixture, because when gas mixture be pre-chilled to above zero, below 10 ℃ the time, most of moisture in the gas mixture atomizes, and can remove through gas-liquid separation.Preferred precooling temperature is controlled between 2 ℃～6 ℃.
The gas composition of gained after above-mentioned secondary gas-liquid separation wherein also contains carburet hydrogen trace, that do not liquefy.Because the emission standard of different areas may be different, thereby can carry out solvent absorbing or charcoal absorption processing to this gas composition, with the hydrocarbon content in the further reduction emission gases according to practical situation.After method processing of the present invention, the hydrocarbon content of emission gases generally will be lower than national specified discharge standard 150mg/Nm
3Another scheme is with the gas composition of gained after the secondary gas-liquid separation combustion air as torch in refinery or other device, carries out burn processing.
In fact, hydro carbons and Air mixing gas can carry out pressurized treatment in the step (a) before precooling.Pressurized treatment can adopt compressor, and it is 0.3-1.0MPa that hydro carbons and Air mixing gas are compressed to gauge pressure, is preferably 0.4-0.8MPa.Pressure-fired can adopt blower fan.
The secondary gas-liquid separation afterwards of elementary gas-liquid separation in the step (b) and/or step (c) adopts ultra-filtration equipment to carry out.Ultra-filtration equipment is made the separator of filtration medium by sintered stainless steel silk felt and/or is made up of the separator that beta glass fibre is made filtration medium.The filtration of ultra-filtration equipment belongs to coefficient Depth Filtrations of association mechanism such as diffusion, interception, collisions, can effectively capture sub-micron grade particle.Remaining liquid hydrocarbon content can be less than 1mg/m in the gas phase
3, filtering accuracy reaches 10 nanometers.The filter core of ultra-filtration equipment can be a round barrel shape filter bed structure, and filter bed is made up of pre-filtering layer, ultra-fine fibre layer, transition layer and gravity settling layer.After the liquid particle that is suspension enters the ultra-fine fibre layer, small oil gas sol particles is under the comprehensive actions such as direct interception, inertial impaction and pedesis of intensive fibre bed, be collected in one by one on the ultra-fine fibre, and be tending towards assembling, cohesion and produce gravity settling.
In elementary gas-liquid separator, adopt above-mentioned ultra-filtration equipment efficiently, can be under the higher precooling temperature as above zero, below 10 ℃, remove most moisture, eliminated the icing hidden danger in the rerigerator; And in the secondary gas-liquid separator, adopt ultra-filtration equipment efficiently, can under higher relatively temperature, reclaim liquid hydrocarbon, thereby reach purpose of energy saving.In the present invention, preferred deep cooling condensing temperature is controlled between-20 ℃～-40 ℃.
In addition, in the step (b) through the gas composition of elementary gas-liquid separation before carrying out deep cooling, can use molecular sieve adsorption, membrane sepn or defrost liquid further to remove wherein moisture, to reduce the accumulation of icing in the rerigerator.Defrost liquid generally adopts alcohols.
The present invention also provides a kind of device that reclaims hydro carbons from hydro carbons and Air mixing gas, and this device both can be placed on the skid plate formula bearing base that can move, and also can be fixed in field ground, and its main integral part comprises according to priority:
(1) precooler;
(2) elementary gas-liquid separator;
(3) deep condenser.
After deep condenser, also can be connected to the secondary gas-liquid separator.
Also can link before precooler has compressor or blower fan, so that for system provides supercharging, is that gas flow provides power in the system, also may improve separating effect simultaneously.
And said elementary gas-liquid separator and/or secondary gas-liquid separator can be made of ultra-filtration equipment, make the separator of filtration medium and/or the separator that beta glass fibre is made filtration medium and ultra-filtration equipment comprises sintered stainless steel silk felt.
Among the present invention, before said deep condenser, also can link moisture eliminator, membrane separation apparatus that molecular sieve is housed or the defroster that defrost liquid is housed, to carry out deep dehydration.
Precooler can adopt surplus cold heat exchanger, promptly utilizes the emission gases that disposes to cool off hydro carbons and the initial logistics of Air mixing.The rerigerator that can certainly use hydrocarbon compound to make cooling agent carries out pre-cooled.
Deep condenser then can use hydrocarbon compound to make the rerigerator of cooling agent, so that reach the low temperature that hydro carbons is reclaimed in condensation.
In apparatus of the present invention, can link active carbon adsorber, solvent absorbing tower or combustion unit after the secondary gas-liquid separator, hydrocarbon content reaches emission standard or is better than emission standard in the gas of feasible final discharging.
In method and apparatus of the present invention,, especially adopt ultra-filtration equipment as elementary gas-liquid separation device, and eliminated the icing blockage problem in the rerigerator owing to adopt the elementary gas-liquid separation of pre-cold-peace; And the secondary gas-liquid separation of employing ultra-filtration equipment makes the temperature of deep cooling condensation can improve relatively again, thereby has reduced energy consumption.
Further set forth the present invention by accompanying drawing with embodiment below, but scope of the present invention is not limited only to these embodiment.These embodiment implement part optimal way of the present invention.
Fig. 1 is can schematic flow sheet site-assembled, recovery hydro carbons from hydro carbons and Air mixing gas.
Fig. 2 be adopt membrane separation apparatus, can be site-assembled, the schematic flow sheet that from hydro carbons and Air mixing gas, reclaims hydro carbons.
Fig. 3 is packaged type reclaims hydro carbons from hydro carbons and Air mixing gas a schematic flow sheet.
Wherein, the 1st, the oil gas collection device, the 2nd, be used for the surplus cold heat exchanger of precooling, the 3rd, elementary gas-liquid separator (ultra-filtration equipment), the 4th, interchanger, the 5th, be used for the rerigerator of deep cooling condensation, the 6th, active carbon adsorber, the 7th, rubbing property gas tank, the 8th, compressor, the 9th, sled seat, the 10th, membrane separation apparatus or mole sieve drier, the 11st, secondary gas-liquid separator (ultra-filtration equipment), the 12nd, solvent absorbing tower.
Embodiment 1
After hydro carbons and Air mixing gas are collected,, enter compressor 8 through rubbing property gas tank 7 bufferings in 1.Gas mixture after the supercharging carries out precooling in surplus cold heat exchanger 2, the temperature of precooling is controlled at 3～5 ℃; Gas mixture after the precooling carries out elementary gas-liquid separation in ultra-filtration equipment, remove the water and the part heavy hydrocarbon of wherein atomizing, the gas composition that comes out from 3 is further cooling in interchanger 4, to make full use of the surplus cold of system, enter the rerigerator 5 of making cooling agent with propylene afterwards again, carry out the deep cooling condensation, condensing temperature is controlled at about-40 ℃, isolate the hydrocarbon of liquid, handle, further remove the micro-hydrocarbon in the gas composition and the gas composition of separating enters active carbon adsorber 6; After measured, hydrocarbon content is lower than 120mg1Nm in the gas of discharging
3Gas composition is before discharging, through interchanger 4 and surplus cold heat exchanger 2 recovery cold wherein, to cut down the consumption of energy.
Ultra-filtration equipment 3 is made of the two-stage separating and filtering device, and first step filter material is a sintered stainless steel silk felt, and second stage filter material is a mean diameter less than 1 micron beta glass fibre.
Embodiment 2
The technical process of present embodiment is identical with embodiment 1, but this flow process does not have the interchanger 4 among the embodiment 1, simultaneously after ultra-filtration equipment 3, insert a membrane separation apparatus or mole sieve drier 10 before the rerigerator 5, further to remove the moisture in the gas composition that enters rerigerator 3.
Embodiment 3
The technical process of present embodiment is identical with embodiment 1, but changes active carbon adsorber 6 into solvent absorbing tower 12, simultaneously after rerigerator 5, before the solvent absorbing tower 12, insert a secondary gas-liquid separator 11 that is made of ultra-filtration equipment.In addition, all devices of present embodiment all is fixed on the skid plate formula bearing base, moves with convenient.The structure of the elementary gas-liquid separator 3 among the structure of secondary gas-liquid separator 11 and the embodiment 1 is identical.Because present embodiment has adopted secondary gas-liquid separator 11, the condensing temperature of rerigerator 5 can be controlled in about-30 ℃.
Claims (18)
1. method that reclaims hydro carbons from hydro carbons and air Mixture comprises following process:
(a) hydro carbons and Air mixing gas are carried out precooling, precooling temperature is controlled at above zero, below 10 ℃;
(b) gas mixture after the precooling in (a) is carried out elementary gas-liquid separation, isolate wherein formed liquid phase composition;
(c) will carry out the deep cooling condensation through the gas composition after the elementary gas-liquid separation in (b), condensing temperature is controlled at-10～-70 ℃, reclaims wherein formed liquid hydrocarbon.
2. the method for claim 1 is characterized in that, after said deep cooling condensation, adopts secondary gas-liquid separator recovering liquid hydrocarbon.
3. method as claimed in claim 2 is characterized in that the gas composition of gained carries out solvent absorbing, charcoal absorption or burn processing, emptying then after the secondary gas-liquid separation.
4. as claim 2 or 3 described methods, it is characterized in that hydro carbons and Air mixing gas carried out pressurized treatment in the step (a) before precooling.
5. method as claimed in claim 4 is characterized in that, said pressurized treatment is to adopt compressor, and with said gas mixture compress to gauge pressure be 0.3-1.0MPa.
6. method as claimed in claim 4 is characterized in that, said pressurized treatment is to adopt blower fan.
7. as claim 2 or 3 described methods, it is characterized in that said precooling temperature is controlled between 2～6 ℃ in the step (a).
8. as claim 2 or 3 described methods, it is characterized in that said elementary gas-liquid separation and/or said secondary gas-liquid separation are to adopt ultra-filtration equipment to carry out gas-liquid separation.
9. as claim 2 or 3 described methods, it is characterized in that, in the step (b) through the gas composition of elementary gas-liquid separation before carrying out deep cooling, further remove wherein moisture content with molecular sieve adsorption, membrane sepn or defrost liquid.
10. as claim 2 or 3 described methods, it is characterized in that said deep cooling condensing temperature is controlled between-20～-40 ℃ in the step (c).
11. a device that reclaims hydro carbons from hydro carbons and Air mixing gas can be made the skid plate formula that can move, and also can be fixed in field ground, it comprises according to priority as the lower section:
(1) precooler;
(2) elementary gas-liquid separator;
(3) deep condenser.
12. device as claimed in claim 11 is characterized in that, after said deep condenser, also is connected to the secondary gas-liquid separator.
13. device as claimed in claim 12 is characterized in that, this device also included compressor or blower fan before said precooler.
14. as claim 12 or 13 described devices, it is characterized in that, said elementary gas-liquid separator and/or secondary gas-liquid separator are made of ultra-filtration equipment, and this ultra-filtration equipment comprises that sintered stainless steel silk felt makes the separator of filtration medium and/or the separator that beta glass fibre is made filtration medium.
15. device as claimed in claim 14 is characterized in that, links the defroster that moisture eliminator, the membrane separation apparatus of molecular sieve is housed or defrost liquid is housed before said deep condenser.
16. device as claimed in claim 15 is characterized in that, said precooler is the rerigerator that surplus cold heat exchanger or hydrocarbon compound are made cooling agent.
17. device as claimed in claim 16 is characterized in that, said deep condenser is the rerigerator that hydrocarbon compound is made cooling agent.
18. device as claimed in claim 17 is characterized in that, this device links active carbon adsorber, solvent absorbing tower or combustion unit after the secondary gas-liquid separator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01100559 CN1366021A (en) | 2001-01-15 | 2001-01-15 | Process and apparatus for recovering hydrocarbons from hydrocarbon and air mixed gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01100559 CN1366021A (en) | 2001-01-15 | 2001-01-15 | Process and apparatus for recovering hydrocarbons from hydrocarbon and air mixed gas |
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| Publication Number | Publication Date |
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| CN1366021A true CN1366021A (en) | 2002-08-28 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 01100559 Pending CN1366021A (en) | 2001-01-15 | 2001-01-15 | Process and apparatus for recovering hydrocarbons from hydrocarbon and air mixed gas |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101555415B (en) * | 2009-05-18 | 2013-04-03 | 青岛华世洁环保科技有限公司 | Method and apparatus for recovering oil product from oil-containing mixed gas |
| CN103100236A (en) * | 2013-03-08 | 2013-05-15 | 庞世花 | Oil gas recovery method |
| CN104083981A (en) * | 2014-07-02 | 2014-10-08 | 天津大学 | Direct-contact-type deep cooling device for recycling volatile organic compound waste gas and recycling method |
| CN105344201A (en) * | 2015-11-16 | 2016-02-24 | 广东上典环境保护工程有限公司 | Organic waste gas recovery method based n condensation-extraction process |
| CN107129826A (en) * | 2017-05-11 | 2017-09-05 | 蚌埠市荣强压缩机制造有限公司 | A kind of device for recovering oil and gas for gas station |
| CN107215841A (en) * | 2017-06-14 | 2017-09-29 | 蚌埠市荣强压缩机制造有限公司 | A kind of device for recovering oil and gas for gas station |
| CN107267188A (en) * | 2017-05-11 | 2017-10-20 | 蚌埠市荣强压缩机制造有限公司 | A kind of gas station oil gas retracting device |
| CN110452730A (en) * | 2019-09-02 | 2019-11-15 | 上海优华系统集成技术股份有限公司 | The recovery system and its method of heavy constituent in lighter hydrocarbons dry gas |
-
2001
- 2001-01-15 CN CN 01100559 patent/CN1366021A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101555415B (en) * | 2009-05-18 | 2013-04-03 | 青岛华世洁环保科技有限公司 | Method and apparatus for recovering oil product from oil-containing mixed gas |
| CN103100236A (en) * | 2013-03-08 | 2013-05-15 | 庞世花 | Oil gas recovery method |
| CN104083981A (en) * | 2014-07-02 | 2014-10-08 | 天津大学 | Direct-contact-type deep cooling device for recycling volatile organic compound waste gas and recycling method |
| CN104083981B (en) * | 2014-07-02 | 2016-04-20 | 天津大学 | The straight touch degree of depth cooling device that volatile organic compound from waste gas reclaims and recovery method |
| CN105344201A (en) * | 2015-11-16 | 2016-02-24 | 广东上典环境保护工程有限公司 | Organic waste gas recovery method based n condensation-extraction process |
| CN105344201B (en) * | 2015-11-16 | 2018-01-30 | 广东上典环境保护工程有限公司 | Based on condensation abstraction method method for organic waste gas recovery |
| CN107129826A (en) * | 2017-05-11 | 2017-09-05 | 蚌埠市荣强压缩机制造有限公司 | A kind of device for recovering oil and gas for gas station |
| CN107267188A (en) * | 2017-05-11 | 2017-10-20 | 蚌埠市荣强压缩机制造有限公司 | A kind of gas station oil gas retracting device |
| CN107215841A (en) * | 2017-06-14 | 2017-09-29 | 蚌埠市荣强压缩机制造有限公司 | A kind of device for recovering oil and gas for gas station |
| CN110452730A (en) * | 2019-09-02 | 2019-11-15 | 上海优华系统集成技术股份有限公司 | The recovery system and its method of heavy constituent in lighter hydrocarbons dry gas |
| CN110452730B (en) * | 2019-09-02 | 2021-08-06 | 上海优华系统集成技术股份有限公司 | System and method for recovering heavy components in light hydrocarbon dry gas |
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