CN1748835A - Method and process flow for recovering organic matter component from organic exhaust gas - Google Patents
Method and process flow for recovering organic matter component from organic exhaust gas Download PDFInfo
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- CN1748835A CN1748835A CN 200410079996 CN200410079996A CN1748835A CN 1748835 A CN1748835 A CN 1748835A CN 200410079996 CN200410079996 CN 200410079996 CN 200410079996 A CN200410079996 A CN 200410079996A CN 1748835 A CN1748835 A CN 1748835A
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Abstract
The process of recovering organic matter component from exhaust organic gas is suitable for the conditions of relatively small exhaust amount to be recovered and treated, relatively high flow and concentration fluctuation, and dispersed exhaust source. The recovering and treating system includes site parts and movable part. The site parts are set in the gas exhaust sites to accept exhausted gas and adsorb the organic component onto the adsorbent. The movable part may be used to desorb and regenerate saturated absorbent and collect desorbed organic component for several site parts.
Description
Technical field
The present invention relates to a kind of method and technological process of from the organic gas of discharging, reclaiming organic matter component.Particularly from the volatile organic matter gas that the emission source that gas emissions is less relatively, discharge capacity is unstable, emission point disperses gives off, reclaim volatile organic matter, and make the method and the technological process of the tail gas cleaning discharging after the processing.
Background technology
Often run into the gas emission problem of volatile organic matter many industry and commercial field people.This class gas one or more VOC components (hereinafter to be referred as organic matter component) that normally boiling point is not too high or mix the mist that forms (below be referred to as organic exhaust gas) with inert gas by a certain amount of above-mentioned organic matter component, normal temperature, normal pressure and with the inert gas admixture under, these organic matter components are gaseous state, and remaining organic matter component is being liquid after removing wherein inert gas under normal temperature and the certain pressure or under normal pressure and the low temperature.Organic matter in this type organic emission gases is reclaimed to get off to be used or reasonably dispose, not only can reduce the waste of resource, and can reduce, can also reduce the danger of breaking out of fire and blast simultaneously to the injury of human body with to the pollution of atmosphere.
The method of handling these organic exhaust gas at present mainly contains absorption method, absorption process, condensation method and oxidation burning method etc.The basic principle of absorption method is, utilize solid absorbent surface different to the absorption of different material in the emission gases and desorption ability, organic matter component in the organic exhaust gas is adsorbed on the surface of adsorbent, enter atmosphere and will remove the inert gas that is not adsorbed behind the organic matter component, when adsorbent reaches certain absorption saturation degree, again adsorbent is carried out desorption and regeneration, the organic matter component desorption that is adsorbed on the adsorbent is got off, make adsorbent recover adsorption capacity again.Though this method adsorption process is fairly simple, absorption back discharge tail gas concentration is low, and desorption process is more loaded down with trivial details, and absorption and desorption process need at least two equipment handover operations, thus to the requirement of control section also than higher.The basic principle of absorption process is, make organic exhaust gas pass the absorption tower of loading column plate or filler from bottom to up, with top-down organic matter liquid-absorbant counter current contacting on column plate or filler, organic matter component in the emission gases is absorbed agent and absorbs, enter atmosphere through the tail gas that absorbs after handling from cat head, the rich absorbent that has absorbed organic matter component then in follow-up desorption process by desorb, absorbent after the desorb recovers absorbability and returns the absorption tower to recycle again, and the organic matter component that desorbs is further absorbed or be condensed into liquid by another kind of absorbent again.The major defect of absorption process is to absorb back exhaust emissions concentration often than higher.The condensation ratio juris is, directly the temperature with organic exhaust gas is reduced to below the dew point of organic matter component, makes organic matter component be condensed into liquids recovery and gets off, and condensed tail gas directly discharges.The disadvantage of condensation method be energy consumption than higher, especially the organic exhaust gas concentration ratio is lower, needs again simultaneously to satisfy when requiring than higher exhaust emissions, needs all emission gases are cooled to very low temperature, causes energy consumption for cooling significantly to increase.The burning ratio juris is, having under the condition that catalyst exists or catalyst-free exists, directly enter atmosphere after making organic matter component generation oxidation reaction in the organic exhaust gas generate carbon dioxide and water, though oxidizing process is simple, but mixed gas flow and steady concentration and continuity are required than higher, and organic matter can not obtain recycling in addition.Said method respectively has pluses and minuses when handling the various organic exhaust gas that discharge capacity is bigger and discharge capacity is more stable.
But, for handle discharge capacity compare less, or discharge capacity or the concentration of emission fluctuation ratio is big even intermittent discharge, or public work is when relying on the organic exhaust gas of the not so good occasion of condition, said method all faces common problem again in varying degrees.At first be the investment that how to reduce retracting device, make recycling and processing device can satisfy the maximum requirement of handling load, can therefore not produce excessive investment again; Next is how to reduce operation and maintenance cost effectively, and particularly in discharge capacity or concentration of emission fluctuation ratio during big even intermittent discharge, the operation and maintenance cost of recycling and processing device still can keep lower level; Organic matter component concentration is enough low in the tail gas of discharging after guaranteeing again simultaneously to handle, and the rate of recovery is enough high in other words.Do not find a kind of efficient ways and technological process just, the organic exhaust gas that up to the present a lot of enterprises have to produce directly enters atmosphere, causes the waste and the environmental pollution of resource.
Goal of the invention
The objective of the invention is to propose a kind of compare less or flow and fluctuation of concentration is bigger, emission source disperses organic exhaust gas of discharge capacity to be recycled, and make the tail gas of discharging after treatment satisfy recovery processing technique method than higher emission request.
Another object of the present invention is to propose compare less or flow and fluctuation of concentration is bigger, emission source disperses organic exhaust gas of discharge capacity recycled, and makes the satisfied recovery processing technique flow process than higher emission request of the tail gas of discharging after treatment.
A further object of the invention is to propose a kind of output investment ratio is lower, operation and maintenance cost is lower processing discharge capacity compare less or flow and fluctuation of concentration is bigger, emission source disperses organic exhaust gas, and makes the tail gas of discharging after treatment satisfied recovery processing technique method and technological process than higher emission request.
Summary of the invention
The recycling discharge capacity that the present invention proposes compares less or flow and fluctuation of concentration is bigger, the method for the organic exhaust gas of emission source dispersion is to realize by the recycling system that is made of jointly in two sub-sections situ part and moving part.Situ part wherein receives the organic exhaust gas that emission source is discharged at any time, and with the method for absorption organic matter component wherein is adsorbed on the surface of adsorbent, allows enter atmosphere through the cleaning tail gas after the adsorption treatment; Movable part wherein can be more than one situ part the regeneration service is provided, when the adsorbent of a certain situ part reaches certain absorption saturation degree and need regenerate, movable part is moved to the scene, connect flow process, movable part can provide necessary regeneration condition for situ part, adsorbed organic matter component desorption on the adsorbent in the situ part adsorption tanks is got off, make adsorbent obtain regeneration, meanwhile, movable part reclaims the organic matter component that desorption comes out get off, so that focus utilization or disposal.
The benefit of the method for this recycling organic exhaust gas is conspicuous.Situ part adopts the method for absorption can guarantee to reach enough low concentration of emission through absorption back discharge tail gas; The fixing adsorption tanks of situ part can receive at any time than small emission or discharge capacity and concentration of emission to be had than great fluctuation process, even the organic exhaust gas of intermittent discharge; Adsorption process does not need the external world that power is provided basically, do not have power consumption substantially, so operating cost is low; Because situ part only need be provided with less, the simple adsorption plant of flow process of investment, and investment regeneration recovery section big, the flow process relative complex can be respectively a plurality of situ parts service is provided, in fact its investment is shared by a plurality of situ parts, so the output investment ratio of whole recovery system after sharing is lower; Concentrate the recovery organic matter component also to be convenient to focus utilization or disposal in addition.
Compare less or flow and fluctuation of concentration is bigger, emission source disperses organic exhaust gas of the said discharge capacity of the present invention refers to, total amount of organic in the organic exhaust gas recycles not enough economical rationality because of small scale with existing method, or more reasonable economically with method recycling of the present invention; Or the flow of organic exhaust gas and concentration are difficult to adopt existing processed continuously method that it is recycled effectively because of fluctuation; The emission source of these organic exhaust gas of while apart from each other again is difficult to put together with pipeline.
The said organic exhaust gas of the present invention refers to such an extent that be organic matter one-component or gas mixture, or the mist of organic matter one-component or mixture and inert gas, organic matter one-component wherein or mixture can be adsorbed agent at normal temperatures and pressures and adsorb well, and under the pressure condition of environment temperature and 1～110mmHg (absolute pressure) can by effectively from the adsorbent desorption come out, be that normal temperature～-40 ℃ and pressure are can be liquefied under the condition of 0～4.0MPa (gauge pressure) to be organic matter liquid in temperature simultaneously.These organic matters may be the resources of recyclable utilization, or directly enter the atmosphere human body and suck the harmful noxious material in back, or directly enter the pollutant that atmosphere can cause air environmental pollution, or directly enter the dangerous material that atmosphere can increase fire and explosive hazard, or above-mentioned situation has concurrently.Inert gas in the organic exhaust gas refers to such an extent that be that air, nitrogen, water etc. enter the gas that can not cause direct pollution behind the atmosphere to environment.
Situ part
The major function of situ part is to realize by the adsorption tanks that loading solid absorbent that fixedly mounting.Utilize the adsorbent in the adsorption tanks that organic matter component in the emission gases and inert gas are adsorbed the different characteristics of affinity, to be adsorbed onto on the surface of adsorbent by the organic matter component in the organic exhaust gas of adsorption tanks at any time, the tail gas that the organic matter component that is not adsorbed by inert gas that is not adsorbed and minute quantity is formed then passes the adsorbent bed atmosphere that enters.
When the adsorbent in the adsorption tanks reaches certain absorption saturation degree and need regenerate, the flow process of situ part is switched to reproduced state, simultaneously flow process is communicated with movable part, adsorbent surface adsorbed organic matter component desorption in the adsorption tanks is come out by the negative pressure that movable part provides.Situ part also should have can introduce the organic exhaust gas of discharging at adsorption tanks regeneration period emission source the flow process of the back adsorption tanks of movable part, can both obtain recycling so that comprise the organic exhaust gas whenever emission source is discharged in desorption stage.In addition, on the inlet takeoff line of emission source and adsorption tanks, the line of releasing should be set,, guarantee that exhaust system can build the pressure or vacuum at no time on the line of releasing by safety relief mechanism is set.
Therefore, the technological process of situ part should comprise the adsorption tanks that loading adsorbent at least; The takeoff line that connects emission source and adsorption tanks inlet; Connect the drop out line of adsorption tanks to atmosphere; Be communicated with adsorption tanks and have the regeneration line of the connector that the vacuum unit arrival line with movable part connects; Be connected on the takeoff line between emission source and the adsorption tanks and have the regeneration takeoff line of the connector that the pipeline with the back adsorption tanks inlet of movable part connects; Be connected the line of releasing that has safety relief mechanism on the takeoff line; And relevant valve, instrument etc.
The adsorbent of filling can be the various solid absorbents that have than bigger serface in the adsorption tanks, as active carbon, activated alumina, molecular sieve, diatomite, silica gel etc., the any adsorbent of concrete selection need be according to the character of organic matter component in the emission gases, absorption and the desorption performance of organic matter component on adsorbent, the adsorption capacity of adsorbent, combined factors such as adsorbent service life and price and deciding.
The loadings of adsorbent can be according to the organic average quality flow rate of emission source discharge in the adsorption tanks, the adsorption capacity of adsorbent, and factors such as regeneration interval are determined.For building up and just at operating adsorption tanks, when need regeneration, can calculate according to regenerate for the last time organic exhaust gas amount and the concentration of post processing of sorbent used adsorption capacity and adsorption tanks, or determine according to the tail gas concentration determination of adsorption tanks exhaust port.
Movable part
The main task of movable part provides necessary condition of negative pressure, adsorbed organic matter component desorption on the adsorbent in the situ part adsorption tanks is come out, then its condensation is reclaimed, will adsorb again through the on-condensible gas after the recycling at last, make the tail gas emptying of cleaning.
Movable part comprises at least three unit: promptly vacuum unit, reclaim unit and back absorbing unit.
Vacuum unit
The function of vacuum unit mainly is that the adsorbent for needs regeneration provides necessary condition of negative pressure, so that organic matter component desorption from the adsorbent surface gets off, after vacuum unit boosts, sends into the subsequent recovery unit.
The required pressure that provides of vacuum pump inlet, i.e. desorption pressure, relevant with the concentration of discharging tail gas after the absorption of the character of organic matter component and requirement.In general, the compound adsorption capacity that same molecular structural molecule amount is big more is strong more, and the desorption difficulty is big more, and the required pressure of desorption is just low more; In other words, under the identical situation of other operating condition, desorption pressure is low more, the residual organic component is just few more in the adsorbent surface hole of regeneration back, regenerate just thoroughly more, during adsorption operations, the content of organics of absorption back discharging tail gas is just low more so again.But then, desorption pressure is low more, and equipment investment and operating cost are high more.Because the pressure of adsorption tanks reduces gradually in the desorption process, said here desorption pressure is meant the minimum pressure that desorption process later stage vacuum pump inlet reaches.
When containing oxygen in the mist that desorption comes out, for safety, usually can select liquid-ring vacuum pump as vaccum-pumping equipment, at this moment vacuum pump inlet pressure is subjected to the restriction of the saturated vapour pressure of circulation fluid (or claiming sealing liquid), generally at 30～110mmHg, more at 50～80mmHg, under this pressure, the most organic component can come out from desorption on the adsorbent.When the lower desorption pressure of needs, can select other vacuum equipment for use, in any case but desorption pressure should not be lower than 1mmHg, otherwise, even vacuum equipment can reach, also often be difficult to feasible economically.Therefore, in general desorption pressure should be chosen in 1～110mmHg scope.
Vaccum-pumping equipment can also adopt centrifugal vacuum pump, screw vavuum pump, rotary-vane vaccum pump, reciprocating vacuum pump, jet pump etc. except adopting liquid-ring vacuum pump, also can be their combination.
In the desorption process from the gas of adsorption tanks except the organic matter component that desorption from adsorbent surface comes out, also have the inert gas that is present in before the desorption in the adsorption tanks.Therefore, in fact the gas that enters movable part from situ part in the desorption and regeneration process is the mist of organic matter component and inert gas, and just concentration is higher, and its volumetric concentration reaches 85～95% usually, is called the organic matter enriched gas below therefore.At vacuum unit, the organic matter enriched gas is after vavuum pump boosts and is cooled, and a part of organic matter component wherein may be condensed into liquid, is separated at vacuum unit.Organic concentration is relatively low in the organic matter enriched gas, and organic matter component is low weight, and chilling temperature is when higher, and the organic matter amount of liquid that vacuum unit condenses is just fewer; Otherwise organic concentration is higher relatively in the organic matter enriched gas, and organic matter component is heavier, and chilling temperature is when relatively low, and the organic matter amount of liquid that vacuum unit condenses is just many.
Reclaim the unit:
The major function that reclaims the unit is by reducing the method for condensation temperature or raising condensing pressure, to separate with inert gas from the organic matter component in the organic matter enriched gas of vacuum unit, recovery obtains organic matter liquid, and on-condensible gas is drained into the back absorbing unit.
According to the principle that balances each other, the organic matter component boiling point in the organic matter enriched gas is low more, and concentration is low more, and required condensation temperature is low more, and condensing pressure is high more.For the organic matter enriched gas of definite composition and concentration, condensation temperature is low more, and it is also low more then to reach the required condensing pressure of the identical rate of recovery; Otherwise condensation temperature is high more, and it is also high more then to reach the required condensing pressure of the identical rate of recovery.Therefore reclaiming the unit, can to adopt the condensation temperature that reduces organic matter enriched gas condensation process be the low-temperature atmosphere-pressure condensation process, or to improve condensing pressure be normal temperature compressed condensation process, or to reduce condensation temperature simultaneously and improve condensing pressure be the purpose that low temperature compression condensation technology realizes organic matter component is condensed into liquid.Concrete what kind of condensation process of employing and operating condition need be according to the compositions of organic matter component, and the concentration of organic matter component in the organic matter enriched gas reclaims the unit and wishes that the factors such as the rate of recovery that reach are comprehensive definite after calculating.Calculate according to the processing simulation that the inventor did, generally, when reclaiming unit employing low-temperature atmosphere-pressure condensation process, condensation temperature should be at-10～-40 ℃, and condensing pressure is an atmospheric pressure; When adopting normal temperature compressed condensation process, condensation temperature is a normal temperature, and condensing pressure should be in 1.0～4.0MPa (gauge pressure); When adopting low temperature compression condensation technology, condensation temperature should be at 10～-20 ℃, and condensing pressure should be in 0.5～2.0MPa (gauge pressure).Too high or the condensing pressure of condensation temperature cross low can cause hydrocarbon component reclaim the unit can not be by abundant condensation; And condensation temperature is crossed the increase that the low or too high meeting of condensing pressure causes equipment investment and operating cost.
Owing to contain a certain amount of moisture content usually in the organic matter enriched gas, when the condensation temperature that reclaims the unit is lower than 0 ℃, condensation process need be divided into two stages, phase I wherein is precooling, condensation temperature is 0～5 ℃, main purpose is that the most of moisture content condensation in the organic matter enriched gas is got off, and prevents to block because of too fast frosting causes equipment in the cryogenic condensation stage at rear portion; Second stage is a cryogenic condensation, is condensed at this at uncooled organic matter component of precooling stage.Nonetheless, during cryogenic condensation, condenser still needs to defrost in good time.
The organic matter liquid that recovery unit condensation obtains is admitted to the storage of organic matter wet tank.
Back absorbing unit:
Leave in the on-condensible gas that reclaims the unit and still contain the organic matters component, the purpose that the back absorbing unit is set be with the organic exhaust gas that this part gas and adsorption tanks regeneration period emission source are discharged merge introduce after adsorption tanks carry out adsorption treatment, make the cleaning tail gas qualified discharge after the processing.
Back absorbing unit mainly is the back adsorption tanks that solid absorbent is being loaded in an inside, when on-condensible gas pass the back adsorption tanks adsorbent bed the time, organic matter component in the on-condensible gas is attracted on the surface of adsorbent, and the tail gas that regenerative process is discharged finally reaches emission request too.The adsorbent of back absorbing unit can adopt the various solid absorbents that are suitable for organic matter component absorption and desorption equally, as: active carbon, activated alumina, molecular sieve, diatomite, silica gel etc.
After the adsorption tanks of several situ parts are carried out desorption and regeneration, when the adsorbent when the back in the adsorption tanks reaches certain saturation degree, can regenerate to it with the desorption and regeneration flow process of movable part self, regenerative process is similar to the regenerative process of adsorbent in the situ part adsorption tanks, different is to carry out last adsorption treatment with reclaiming the on-condensible gas introducing situ part adsorption tanks of discharging the unit this moment, cleans tail gas at last and enters atmosphere.Whole like this emission gases can both enter atmosphere through after the adsorbents adsorb.
For realizing the above-mentioned task of movable part, except above-mentioned vacuum unit, reclaim unit and the back absorbing unit, the technological process of movable part at least also should comprise the regeneration line that is communicated with vacuum pump inlet and has the connector that the regeneration line with situ part connects; Back adsorption tanks are to the drop out line of atmosphere; Be connected on the adsorption tanks suction line of back and have the regeneration takeoff line etc. of the connector that the regeneration takeoff line with situ part connects.
When practical application, the movable part assembling is as a whole, and with motor vehicle or the delivery of other vehicles, the energy that provides with the scene or delivery vehicle self provides is made operation power, can be called the regeneration recovery machine that moves.One is moved the situ part that regeneration recovery machine can be the same or similar character organic matter component of a plurality of dischargings gas service is provided, and organic matter liquid focus utilization or disposal that recovery is obtained.
Below be schematic flow sheet and embodiment for explaining that purpose of the present invention and principle propose.Need to prove that flow process of the present invention and embodiment can have multiple specific implementation, scope of the present invention can not be understood that to only limit to following flow process and embodiment.
Description of drawings
Scheme the-1st, comprise the main-process stream block diagram of situ part and movable part.
Figure the-2nd, the schematic flow sheet of situ part.
Figure the-3rd, the movable part schematic flow sheet.
Figure the-4th, the recovery unit schematic flow sheet of employing cryogenic condensation technology.
Figure the-5th, the recovery unit schematic flow sheet of employing compression condensation technology.
The specific embodiment
The invention will be further described below in conjunction with accompanying drawing.
In the technological process general diagram shown in the figure-1, the scope that dot-dash wire frame (1) is enclosed is represented situ part, and the scope that dot-dash wire frame (2) is enclosed is represented movable part.When part was in adsorbed state at the scene, the organic exhaust gas of discharging from emission source entered adsorption tanks by takeoff line (101), and through after the adsorption treatment, cleaning tail gas enters atmosphere through drop out line (102).Movable part is made of vacuum unit, recovery unit and back absorbing unit, during regenerative operation, the regeneration line (201) of movable part docks with the regeneration line (103) of situ part, the regeneration takeoff line (204) of movable part is docked with the regeneration takeoff line (104) of situ part, cleaning tail gas after the back absorbing unit is handled in the regenerative process enters atmosphere by pipeline (203), and the organic matter liquid that obtains in the recovery unit of movable part in the regenerative process is sent by pipeline (202) after finally being transported to and receiving the place.
In the situ part flow process shown in the figure-2, loading adsorbent (106) in the adsorption tanks (105); One end of takeoff line (101) is communicated with emission source, and the other end connects valve (108), and then is communicated with the bottom inlet of adsorption tanks (105) by pipeline (111); One end of drop out line (102) is communicated with adsorption tanks (105) top, and the other end is communicated with atmosphere by valve (112); One end connecting pipeline (111) of regeneration line (103), the other end are provided with the connector (116) that can connect with movable part, and regeneration line (103) is provided with valve (114); One end connecting pipeline (101) of regeneration takeoff line (104), the other end are provided with the connector (117) that can connect with movable part, and regeneration takeoff line (104) is provided with valve (115); An end that is provided with the line of releasing (109) of safety relief mechanism (110) is communicated with takeoff line (101), and the other end is communicated with atmosphere.
Figure the-3rd, the movable part schematic flow sheet.Vacuum unit wherein is mainly by liquid-ring vacuum pump (205), separator (206), sealing liquid pump (207), air cooler (208) and relevant formations such as pipeline valve.The unit is reclaimed in frame of broken lines (250) representative, and figure-4 and figure-5 are respectively the technological processes of adopting the recovery unit of atmospheric low-temperature condensation process and adopting the recovery unit of compression condensation technology.The back absorbing unit mainly back adsorption tanks (209) of adsorbent bed by loading (225) and relevant pipeline valve constitutes.At vacuum unit, an end of regeneration line (201) is provided with the connector (210) that can connect with situ part, and the other end links to each other with the inlet of vavuum pump (205), and the line (201) of regenerating is provided with valve (211).Pipeline (212) is the vacuum pump outlet line, and the one end links to each other with vavuum pump (205) outlet, and the other end is communicated with separator (206).In separator (206) inside, dividing plate (213) is with the container separated into two parts, the circulation sealing liquid (215) (sealing liquid is water and ethylene glycol mixtures) that is in lower floor is blocked on the left side, the organic matter liquid (214) that vacuum pump outlet possibility partial condensation generates then is in the upper strata, and the apical margin that can climb over dividing plate (213) enters the right side.One end of pipeline (217) is communicated with the bottom in separator (206) left side, and the other end connects the inlet of sealing liquid pump (207).The two ends of pipeline (218) are communicated with the outlet of sealing liquid pump (207) and the inlet of air cooler (208) respectively, and pipeline (219) is communicated with the outlet of air cooler (208) with vavuum pump (205), form the closed circuit of sealing liquid.The pipeline (220) of the bottom by being connected separator (206) right side, the organic matter liquid (216) that obtains at vacuum unit can lean on from pressing or importing organic matter wet tank (not drawing among the figure) with the pump back of boosting.Pipeline (221) one ends are communicated with separator (206) top, and the other end links to each other with the recovery unit.Pipeline (202) is the line of sending of the organic matter liquid that reclaims.The on-condensible gas pipeline (222) continuous with reclaiming the unit is being connected valve (223), and be communicated with the back bottom inlet of adsorption tanks (209) by pipeline (224), and with pipeline (203) that adsorption tanks (209) top, back links to each other on valve (226) is installed, the other end of pipeline leads to atmosphere.Pipeline (204) is the regeneration takeoff line, and the one end has the connector (232) that can connect with situ part, and the other end is communicated with pipeline (222).On the pipeline (230) that is provided with for back adsorption tanks regeneration valve (229) is being set, the one end is communicated with pipeline (224), and the other end is communicated with vacuum pump inlet pipeline (201).
In the recovery unit flow process of the employing atmospheric low-temperature condensation process shown in the figure-4, condenser (251) is divided into two chambers by dividing plate (256), the bottom gas phase of two chambers is communicated with, and left chamber is a precooling zone, and its inside is installed with the high temperature cryogen coil pipe (252) of inlaying fin (253); Right chamber is a condensation segment, and its inside is installed with the cryogenic coolant coil pipe (257) of inlaying fin (259) and the heat(ing) coil (258) of defrosting.Organic matter enriched gas from vacuum unit enters condenser by the pipeline (221) that is communicated with precooling zone, enters the back absorbing unit through condensed on-condensible gas by the pipeline (222) that is connected condensation segment.Separator (267) is to be provided with for telling the water that generates when precooling zone condensation and condensation segment defrost.Pipeline (266) is the suction line of separator (267), and the one end is connected the bottom of condenser precooling zone, and the other end is communicated with the middle part of separator (267).When needing, the water (269) in the separator (267) can be discharged by the pipeline (271) and the valve (270) that are installed in the bottom.Be connected on the pipeline (272) at separator (267) top valve (275) is being set, the other end of pipeline is communicated with organic matter wet tank (276), and the organic matter liquid (268) that condensation process obtains can lean on from compressing into into storage tank; The liquid that obtains in the condensation of condenser condenses section also can be by being connected the condensation segment bottom, and the pipeline (274) that is communicated with pipeline (272) and valve (273) flow automatically and enter storage tank.The inlet that is located at the pump (280) of storage tank (276) bottom is communicated with tank bottom by pipeline (278), and outlet can link to each other with the destination storage tank by pipeline (202), when needing, sends after the liquid in the storage tank (276) can being boosted.
Figure the-5th reclaims that the unit adopts normal temperature (or low temperature) compression condensation technology and with the boost compression condensation technology of equipment of liquid-piston compressor conduct.The suction line (221) of compressor (281) is communicated with vacuum unit, and valve (301) is being set on the pipeline, and outlet line (291) is communicated with separator (282).Be provided with return pipeline (290) on compressor import and export pipeline, pressure-regulating valve that is provided with on the pipeline (286) and adjuster (287) constitute the control loop of compressor inlet pressure.Upper strata in the separator (282) is the organic matter liquid (292) that compression condensation generates, and lower floor is the sealing liquid (293) of circulation.The inlet of sealing liquid pump (283) is communicated with separator (282) by pipeline (294), outlet is communicated with the inlet of cooler (284) by pipeline (295), the outlet of cooler (284) is communicated with compressor (281) by pipeline (296), forms the closed circuit of sealing liquid.Said normal temperature compressed condensation refers to such an extent that be that the cooling medium of cooler (284) is a normal temperature; And the low temperature compression condensation refers to such an extent that be that the cooling medium of cooler (284) is a cryogenic coolant.The pipeline (297) that connects separator (282) and storage tank (285) can import storage tank (285) with the organic matter liquid that produces behind the compression condensation, and pipeline (300) then can return the gas in the storage tank separator (282).The other end that is connected the pipeline (222) at separator (282) top is communicated with the back absorbing unit, and pipeline (222) is gone up the pressure-regulating valve (288) of setting and the pressure control loop that adjuster (289) constitutes condenser system.When the organic matter liquid (298) in the storage tank (285) accumulation reaches a certain amount of, can be located at valve (299) on the pipeline (202) by switch, with the organic matter fluid discharge that reclaims to the destination storage tank.Need to prove that the specific implementation of compression condensation can have multiple, adopt the compressor of other pattern or adopt the direct or indirect condensation process of alternate manner can reach purpose of the present invention too.
Below in conjunction with accompanying drawing operating process of the present invention is described.
When being in adsorbed state, valve (114), (115) are closed in the situ part flow process shown in the figure-2, open valve (108), (112), emission gases from emission source enters adsorption tanks (105) via pipeline (101), valve (108) and pipeline (111), when passing adsorbent bed (106), adsorbent absorbs organic matter component wherein, and the cleaning tail gas of removing organic matter component then passes bed, enters atmosphere through pipeline (102) and valve (112).Under the normal condition, release not conducting of safety relief mechanism (110) on the line (109), if because misoperation causes exhaust system to build the pressure and exceeds certain allowed band, the safety relief mechanism (110) on the line of releasing is open-minded, emission gases directly enters atmosphere by the line of releasing (109); Otherwise if exhaust system vacuum occurs and exceeds certain allowed band, air can enter system by line of releasing (109) and the safety relief mechanism (110) that is located on the line of releasing, thereby guarantees unlikely because unexpected superpressure or vacuum are damaged system equipment.
When the adsorbent in the situ part adsorption tanks reaches or when the saturated absorption, need regenerate to the adsorbent in the adsorption tanks.At this moment, movable part moves to the scene, at first connects the power supply of movable part, if reclaim the unit refrigeration system is arranged, and then starts refrigeration system subsequently.(following explanation is as scheming-2 with shown in the figure-3) is connected connector (116) and (210), the regeneration line (103) of situ part and the regeneration line (201) of movable part are communicated with, connect connector (117) and (232), the regeneration line takeoff line (104) of situ part and the regeneration line takeoff line (204) of movable part are communicated with, valve (114) and (115) are opened in valve-off (108), (112); Open valve (211), (231), (223) and (226), valve-off (229); Start pump (207), make the sealing liquid circulation; Start vavuum pump (205), at this moment, the pressure of vavuum pump (205) inlet and adsorption tanks (105) reduces gradually, the organic matter component that is adsorbed on the adsorbent comes out from the adsorbent surface desorption gradually, mix and form the organic matter enriched gas and enter vavuum pump (205) with the inert gas in being present in jar along pipeline (111), (103) and (201), mix with the sealing liquid that enters vavuum pump by the sealing liquid circulatory system, after the process vavuum pump boosts, enter the separator (206) of vacuum unit through pipeline (212).Through vavuum pump boost and the circulate cooling of sealing liquid, may have a certain amount of organic matter component is condensed at vacuum pump outlet and is liquid, owing to have tangible difference in specific gravity and objectionable intermingling between sealing liquid and the organic matter liquid, after the mixed liquor of organic matter liquid and sealing liquid enters separator (206), left side layering at dividing plate (213), the upper strata is an organic matter liquid, and lower floor is a sealing liquid.The sealing liquid of lower floor (215) is extracted out through pipeline (217), after pump (207) boosts, enter air cooler (208) by pipeline (218), the heat that air cooler boosts vacuum unit and condensation process produces all distributes, and cooled sealing liquid circulates again by pipeline (219) and enters vavuum pump (205).Meanwhile, the organic matter liquid (214) on upper strata, separator (206) left side then climbs over the apical margin of dividing plate (213), overflows to the right half part of separator (206).When the operating pressure that reclaims the unit was normal pressure, the organic matter liquid (216) of separator right half part entered the organic matter wet tank (not drawing among the figure-2) that reclaims the unit by pipeline (220) gravity flow; When reclaiming the unit and adopt compression condensation technology, organic matter liquid (216) can be sent into the organic matter wet tank (not drawing among the figure-2) that reclaims the unit after the pump of pipeline (220) by special setting boosts.After the separator separation, the organic matter enriched gas that does not coagulate enters from separator (206) top along pipeline (221) and reclaims unit (250).Reclaiming the unit, organic matter component in the organic matter enriched gas and moisture content are condensed into liquid and obtain reclaiming, uncooled on-condensible gas with regeneration period self-discharging source after the emission gases that regeneration takeoff line (204) is come is mixed after pipeline (222), valve (223) and pipeline (224) enter adsorption tanks (209), adsorbent (225) in the back adsorption tanks (209) absorbs organic matter component wherein, and Qing Jie tail gas enters atmosphere through drop out line (203) and valve (226) at last.When the pressure of situ part adsorption tanks (105) reached the desorption pressure of 80mmHg (absolute pressure), the regenerative operation of situ part finished.Valve-off (114), stop sealing liquid pump (207) and vavuum pump (205), slowly open valve (112), after treating that adsorption tanks (105) recover normal pressure, open valve (108), valve-off (115) disconnects connector (116) and (210), disconnect connector (117) and (232), situ part returns to adsorption operation condition again.
After the regeneration of having carried out several situ parts, the adsorbent in the back adsorption tanks (209) is also saturated near reaching absorption, need regenerate to it.At this moment, valve-off (226), (223) and (211), open valve (229) and (231), connect and be in the connector (117) of the situ part in the adsorption operations and the connector (232) of movable part, (operating process is similar to the regenerative process of aforesaid situ part for the regenerative system of startup movable part, repeat no more) herein, the organic matter enriched gas that desorption comes out is through pipeline (224), valve (229) and pipeline (230), (201) enter vacuum unit, enter the recovery unit subsequently, in this process, organic matter component is condensed into liquids recovery and gets off, the on-condensible gas that is not condensed is then through pipeline (222), (204), valve (231) and valve (115), behind the pipeline (104), with this moment situ part emission gases mix after through pipeline (101), valve (108) and pipeline (111) enter the adsorption tanks (105) of situ part, through after the adsorption treatment, the tail gas of cleaning enters atmosphere through valve (112) and pipeline (102).Equally, when back adsorption tanks (209) regeneration pressure reached desorption pressure about 80mmHg, valve-off (229) stopped vacuum system, slowly opens valve (226), back adsorption tanks (209) recovery normal pressure, back adsorption tanks (209) regeneration ending.
Adopt as scheming the atmospheric low-temperature condensation process shown in-4 if reclaim the unit, during regenerative operation, open valve (273) and (275), the organic matter enriched gas at first enters condenser (251) precooling zone through pipeline (221).At precooling zone, the high temperature cryogen enters along the direction shown in the arrow (254), behind the coil pipe through inlaying fin (253) (252), is returned by the circulation of the direction shown in the arrow (255).When organic matter enriched gas process precooling zone, temperature is reduced to 0～5 ℃, and at this moment, the most of moisture content wherein and the organic matter component of a great deal of are condensed into liquid and drop to the precooling zone bottom, enter separator (267) along pipeline (266).In separator (267), the liquid layering that condensation is got off, the water of bottom (269) is discharged according to liquid level by pipeline (271) by controlled valve (270); The organic matter liquid (268) on top leans on from compressing into into storage tank (276) through pipeline (272) and valve (275).After the organic matter enriched gas from top to bottom passed precooling zone, being turned back by the condenser passage entered condensation segment.At condensation segment, cryogenic coolant enters along the direction shown in the arrow (260), behind the coil pipe through inlaying fin (259) (257), is returned by the circulation of the direction shown in the arrow (261).When the organic matter enriched gas from bottom to top passes through condensation segment, temperature is reduced to-10～-40 ℃, and at this moment, the most of organic matter component in the organic matter enriched gas is condensed into liquid, drop to the condensation segment bottom, enter storage tank (276) along pipeline (274) and pipeline (272).Then enter the back absorbing unit through uncooled on-condensible gas behind the condensation segment by the pipeline (222) at condensation segment top.Regenerative operation stops high low temperature refrigerant cycle after finishing, and movable part is movable to next situ part and carries out another regenerative operation.Although precooling zone gets off the most of moisture content condensation in the organic matter enriched gas, but still has a spot of moisture content can enter condensation segment, and forms frost on the fin of condensation segment, when frosting is seriously arrived to a certain degree, may block condensation segment.At this moment, can be after some regenerative operations finish, stop the circulation of high cryogenic coolant, valve-off (275) is opened the thermit powder circulatory system (not drawing among the figure), and thermit powder passes through heat(ing) coil (258) along the direction shown in arrow (262) and (263), fin (259) is heated, and then with the thawing of the frost on the fin, the water that defrost process generates enters separator (267) along pipeline (274) and (272), finally cuts out by pipeline (271).When the regenerative operation of finishing several situ parts, when the organic matter liquid (277) in the storage tank (276) reaches a certain amount of, movable part is moved to the destination, outlet line (202) is linked to each other with the destination storage tank, reclaim the organic matter liquid that obtains and after pump (280) boosts, be admitted to the destination storage tank by pipeline (278).
Adopt the compression condensation technology shown in the figure-5 if reclaim the unit, during regeneration, open sealing liquid pump (283) and compressor (281), organic matter enriched gas from vacuum unit enters compressor (281) through valve (301) and pipeline (221), sealing liquid with circulation enters compressor, with process that sealing liquid mixes in the organic matter enriched gas cooled off by sealing liquid, wherein the organic matter component of a great deal of is condensed into liquid.Enter separator (282) through the gas-liquid mixture after boosting through outlet line (291).Being located at compressor imports and exports pressure control loop that the pressure-regulating valve (286) that is provided with on return line (290) on the pipeline and the pipeline and adjuster (287) constitute and imports and exports the amount of returning and make compressor inlet pressure keep stablizing by regulating compressor.After entering separator (282), gas-liquid separation, the organic matter liquid (292) in the liquid phase is in the upper strata, enters storage tank (285) through pipeline (297) gravity flow, and meanwhile, the gas in the storage tank (285) returns separator (282) by pipeline (300); The sealing liquid of lower floor (293) enters sealing liquid pump (283) by pipeline (294), and the back of boosting enters cooler (284) cooling by pipeline (295), and when condensation process was normal temperature compressed condensation, the cooling medium of cooler was the normal temperature medium, as air, and recirculated water etc.; When condensation process was the low temperature compression condensation, cooling medium was a cryogenic coolant.Cooled sealing liquid enters compressor (281) by pipeline (296), forms the circulation of sealing liquid.On-condensible gas absorbing unit after pipeline (222) enters of telling from separator (282) top is located at the control loop that voltage-controlled valve (288) on the pipeline (222) and adjuster (289) constitute and has guaranteed the stable of compression condensation process operation pressure.During regeneration ending, stop sealing liquid pump (283) and compressor (281), valve-off (301).When the organic matter liquid (298) in being accumulated in storage tank (285) reaches a certain amount of, movable part is moved to the destination, open valve (299), organic matter liquid is imported the destination storage tank by pipeline (202).
Embodiment
30 average day sale gasoline 12m are arranged
3The gas station, it is 40% oil gas 15m that the average daily discharging in each gas station contains gasoline component volumetric concentration
3(comprising that the oil tank tank car produces gasoline component and Air mixing gas to buried tank emptying and nozzle in the airtight charge of oil process of automotive oil tank), oil gas composed as follows:
| Form | C 1 | C 2 | C 3 | C 3＝ | C 4 | C 4＝ | C 5 | C 6 | C 7 | ＞C 7 | Air | Add up to |
| v％ | 0.1 | 0.2 | 0.6 | 0.6 | 6.5 | 9.0 | 12.0 | 6.0 | 3.0 | 2.0 | 60.0 | 100.0 |
The amount of gasoline that is equivalent to discharge every day each gas station in atmosphere is 19kg.
Adsorption tanks are set, filling 3m in each adsorption tanks in each gas station
3Active carbon as adsorbent, the oil gas (being equivalent to organic exhaust gas) that will discharge from buried tank is introduced adsorption tanks, the cleaning tail gas organic concentration of discharging through adsorbing after is less than 10mg/l, each adsorption tanks was regenerated once in average 5 days.The technological process of situ part is shown in figure-2.
Moving regeneration recovery machine is vehicular, and every is moved the regeneration that regeneration recovery machine is finished 6 gas station's adsorption tanks average every day, can be 30 gas stations service is provided.The flow process that moves regeneration recovery machine is shown in figure-3 and figure-4.The oil gas that comes out from the adsorption tanks desorption with jar in the mean concentration of the mist (organic matter enriched gas) that forms of residual air be 90%, after entering mobile regeneration recovery machine, boost to atmospheric pressure and after separator (206) gas-liquid separation through vavuum pump (205), enter condenser (251) condensation, the temperature of condenser precooling zone is 4 ℃, the temperature of condensation segment is-20 ℃, condensed on-condensible gas again through after after adsorption tanks (209) adsorption treatment, organic concentration enters atmosphere less than the cleaning tail gas of 10mg/l.Every day 6 gas stations regeneration ending after, to the back adsorption tanks carry out primary recycling.The gasoline rate of recovery 99.2% of overall process is equivalent to the average each regeneration in each gas station and reclaims gasoline 94kg, and every is moved regeneration recovery machine and reclaims gasoline 564kg average every day.
Claims (8)
1. a recycling discharge capacity compares less, or flow and fluctuation of concentration are bigger, and the method and the flow process of the organic exhaust gas of emission source dispersion, it is characterized in that: constitute the recycling system jointly by situ part and movable part, situ part wherein is separately positioned on the emission source scene of each organic exhaust gas, at any time receive the organic exhaust gas that emission source is discharged, method with absorption is adsorbed on organic matter component wherein on the surface of adsorbent, allows enter atmosphere through the cleaning tail gas after the adsorption treatment; Movable part wherein can be a plurality of situ parts the regeneration service is provided, when the adsorbent of a certain situ part reaches certain absorption saturation degree and need regenerate, movable part is moved to the scene, connect flow process, movable part provides desorption process required desorption pressure for situ part, adsorbed organic matter component desorption on the adsorbent in the situ part adsorption tanks is got off, make adsorbent obtain regeneration, meanwhile, movable part reclaims the organic matter component that desorption comes out get off, so that focus utilization or disposal; Wherein:
1) flow process of situ part comprises at least:
The adsorption tanks of adsorbent are being loaded in inside;
The takeoff line that connects emission source and adsorption tanks;
Connect the drop out line of adsorption tanks to atmosphere;
Be communicated with adsorption tanks, and the regeneration line of the connector that the regeneration line with movable part connects is arranged;
Be connected on the adsorption tanks inlets takeoff line, and the regeneration takeoff line of the connector that the regeneration takeoff line with movable part connects is arranged;
Be connected on the takeoff line, and have the line of releasing of safety relief mechanism;
2) flow process of movable part comprises at least:
Vacuum unit;
Reclaim the unit;
Back absorbing unit;
Be communicated with vacuum pump inlet, and the regeneration line of the connector that the regeneration line with situ part connects is arranged;
Connect the drop out line of back adsorption tanks to atmosphere;
Be connected on the adsorption tanks suction line of back, and the regeneration takeoff line of the connector that the regeneration takeoff line with situ part connects is arranged.
2. method according to claim 1 is characterized in that: movable part is by motor vehicle or the delivery of other vehicles.
3. method according to claim 1 and flow process, it is characterized in that: said organic exhaust gas is organic matter one-component or gas mixture, or the mist of organic matter one-component or mixture and inert gas, organic matter one-component wherein or mixture can be adsorbed agent at normal temperatures and adsorb well, and under the pressure condition of environment temperature and 1～110mmHg (absolute pressure) can by effectively from the adsorbent desorption come out, be that normal temperature～-40 ℃ and pressure are can be liquefied under the condition of 0～4.0MPa (gauge pressure) to be organic matter liquid in temperature simultaneously.
4. method according to claim 1 and flow process, it is characterized in that: the adsorbent that adopts in adsorption tanks wherein and the back adsorption tanks is an active carbon, or activated alumina, or molecular sieve, or diatomite, or silica gel etc. has bigger specific area and adsorption capacity, is fit to the solid absorbent of organic matter absorption and desorption.
5. according to described method of claim 1 and flow process, it is characterized in that: the scope of desorption pressure is 1～110mmHg (absolute pressure).
6. flow process according to claim 1 is characterized in that: reclaim the unit and adopt the low-temperature atmosphere-pressure condensation process, the condensation temperature scope is-10～-40 ℃, and condensing pressure is a normal pressure.
7. flow process according to claim 1 is characterized in that: reclaim the unit and adopt normal temperature compressed condensation process, condensation temperature is a normal temperature, and the condensing pressure scope is 1.0～4.0MPa (gauge pressure).
8. flow process according to claim 1 is characterized in that: reclaim the unit and adopt low temperature compression condensation technology, the condensation temperature scope is 10～-20 ℃, and the condensing pressure scope is 0.5～2.0MPa (gauge pressure).
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| CN 200410079996 CN1748835A (en) | 2004-09-18 | 2004-09-18 | Method and process flow for recovering organic matter component from organic exhaust gas |
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| CN 200410079996 CN1748835A (en) | 2004-09-18 | 2004-09-18 | Method and process flow for recovering organic matter component from organic exhaust gas |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101637686B (en) * | 2009-09-07 | 2011-10-12 | 孙宗长 | Method for organic waste gas recovery by adopting secondary adsorption |
| CN104587796A (en) * | 2015-01-23 | 2015-05-06 | 马军 | Device for recycling organic solvent from industrial waste gas |
| CN105080181A (en) * | 2014-05-20 | 2015-11-25 | 中石化广州工程有限公司 | Molecular sieve dehydration method for C-4 fraction |
| CN105903311A (en) * | 2016-06-07 | 2016-08-31 | 黎城蓝天燃气开发有限公司 | Gas adsorber and system and method for recycling low-boiling-point organic matter |
| CN105087048B (en) * | 2014-05-20 | 2017-06-20 | 中石化广州工程有限公司 | A kind of method of heavy naphtha molecular sieve dehydration |
| CN109794142A (en) * | 2019-02-04 | 2019-05-24 | 青岛飞普思环保科技有限公司 | The recovery process of oily waste water treatment factory discharge exhaust gas |
| CN109926036A (en) * | 2019-04-18 | 2019-06-25 | 常州大学 | Movable skid-mounted combined type adsorbent desorption and regeneration device on the spot |
| KR20250029761A (en) * | 2024-06-19 | 2025-03-05 | 주식회사 티이씨 | Volatile organic compound recovery method |
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2004
- 2004-09-18 CN CN 200410079996 patent/CN1748835A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101637686B (en) * | 2009-09-07 | 2011-10-12 | 孙宗长 | Method for organic waste gas recovery by adopting secondary adsorption |
| CN105080181A (en) * | 2014-05-20 | 2015-11-25 | 中石化广州工程有限公司 | Molecular sieve dehydration method for C-4 fraction |
| CN105087048B (en) * | 2014-05-20 | 2017-06-20 | 中石化广州工程有限公司 | A kind of method of heavy naphtha molecular sieve dehydration |
| CN105080181B (en) * | 2014-05-20 | 2017-08-22 | 中石化广州工程有限公司 | A kind of method of C-4-fraction molecular sieve dehydration |
| CN104587796A (en) * | 2015-01-23 | 2015-05-06 | 马军 | Device for recycling organic solvent from industrial waste gas |
| CN104587796B (en) * | 2015-01-23 | 2016-09-07 | 马军 | The device of organic solvent is reclaimed from industrial waste gas |
| CN105903311A (en) * | 2016-06-07 | 2016-08-31 | 黎城蓝天燃气开发有限公司 | Gas adsorber and system and method for recycling low-boiling-point organic matter |
| CN105903311B (en) * | 2016-06-07 | 2019-07-12 | 黎城蓝天燃气开发有限公司 | Gas absorber and the system and method for recycling low-boiling-point organic compound |
| CN109794142A (en) * | 2019-02-04 | 2019-05-24 | 青岛飞普思环保科技有限公司 | The recovery process of oily waste water treatment factory discharge exhaust gas |
| CN109926036A (en) * | 2019-04-18 | 2019-06-25 | 常州大学 | Movable skid-mounted combined type adsorbent desorption and regeneration device on the spot |
| KR20250029761A (en) * | 2024-06-19 | 2025-03-05 | 주식회사 티이씨 | Volatile organic compound recovery method |
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