CN1749360A - Process and flow for recovering hydrocarbon component from hydrocarbon containing gas - Google Patents
Process and flow for recovering hydrocarbon component from hydrocarbon containing gas Download PDFInfo
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- CN1749360A CN1749360A CN 200410079995 CN200410079995A CN1749360A CN 1749360 A CN1749360 A CN 1749360A CN 200410079995 CN200410079995 CN 200410079995 CN 200410079995 A CN200410079995 A CN 200410079995A CN 1749360 A CN1749360 A CN 1749360A
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Abstract
Adsorption process is adopted in recovering hydrocarbon component from hydrocarbon containing gas. The working day is divided into two job stages, in the first stage, the first adsorption tank is in adsorption state while the second one in regeneration state; and in the second stage, the second adsorption tank is in adsorption state while the first one in regeneration state. These two long job stages are utilized fully for vacuum and stripping desorption regeneration of these two adsorption tanks and recovering the desorbed hydrocarbon component. Prolonging the desorption regeneration time can reduce the size of the regeneration and recovery parts, lower the investment and the running power consumption.
Description
Technical field
The present invention relates to reclaim in a kind of hydrocarbon component of from lightweight hydrocarbon liquids filling process, overflowing and the Air mixing gas processing method and the technical process of hydrocarbon component.
Background technology
In container (as tank wagon, train tank car or storage tank), filling in the process of light hydrocarbons liquid (as gasoline, kerosene, crude oil, solvent oil, benzene-type products etc.), part hydrocarbon component can evaporate from liquid, form hydrocarbon component and Air mixing gas (hereinafter referred to as hydrocarbon-containifirst gas) with the air that is present in the container, be accompanied by hydrocarbon liquids filling in container, the hydrocarbon-containifirst gas of generation can be forced to discharge container.If it is not recycled, not only cause the waste of resource, also can atmosphere pollution, increase the danger of fire and blast.Since the sixties, making laws one after another and formulate emission standard in countries in the world, limits the uncontrollable discharge of this hydrocarbon-containifirst gas from eighties of last century.All stipulate and to handle the hydrocarbon-containifirst gas of discharging in the light hydrocarbons liquid filling process as most countries and geographic environmental regulation, and the concentration that requires to handle hydrocarbon-containifirst component in the tail gas of discharging the back must not be higher than 10～35mg/l, the country that has, as Germany, the concentration of hydrocarbon-containifirst component must not be higher than 0.15mg/l in the tail gas that environmental regulation even requirement are discharged.
The method of handling hydrocarbon-containifirst gas at present mainly contains absorption method, absorption process, condensation method, membrane separation process, oxidation burning method etc.Exhaust emissions concentration after wherein absorption method is handled with it is low, and many characteristics such as economy and good reliability are the methods that the most generally adopts at present.The earliest and by universally recognized be used for absorption method technology that hydrocarbon gas reclaims be U.S. Pat .Pat.No.4066423 in 1978 propose with absorption method storage tank is breathed the time or the technical process of reclaiming of the hydrocarbon component of the hydrocarbon-containifirst gas of discharging when in container, filling hydrocarbon liquids, after this, U.S. Pat .Pat.No.4276058, US.Pat.No.4462811, US.Pat.No.5480475, patents such as US.Pat.No.5951741 have proposed in succession to the improvement of this absorption method recovery technology and perfect.According to above-mentioned patent and present commercial applications situation, existing absorption method typical process flow is, the hydrocarbon-containifirst confined gas of discharging when filling hydrocarbon liquids is collected, introduce hydrocarbon gas retrieving arrangement (hereinafter referred to as device for recovering oil and gas) by pipeline, the hydrocarbon-containifirst gas that enters device for recovering oil and gas alternately passes two adsorption tanks that loading same amount solid adsorbent (normally gac) bed, what rely on that sorbent material itself had has stronger avidity and air is not almost had the characteristic of avidity hydrocarbon component, make when hydrocarbon-containifirst gas passes the adsorption tanks that are in adsorbed state, hydrocarbon component wherein is attracted to adsorbent surface, and remove hydrocarbon component, main component is an air, and the cleaning tail gas that slightly contains micro-hydrocarbon component then penetrates bed and enters atmosphere.When the sorbent material in the adsorption tanks reaches certain absorption saturation ratio, adsorption tanks are switched to detachment status, the negative pressure that provides by vacuum pump, the hydrocarbon component desorption that is adsorbed on the sorbent material is come out, and the air that retains in the adsorption tanks when hydrocarbon component that desorption comes out and blocked operation forms the higher mixed gas (hereinafter to be referred as the hydro carbons enriched gas) of hydrocarbon-containifirst component concentration.Hydro carbons enriched gas after the process vacuum pump boosts is introduced into the absorption tower, in the absorption tower, hydro carbons enriched gas and the absorption agent of being introduced by the device external system (normally with the identical hydrocarbon liquids of hydrocarbon liquids character that produces hydrocarbon-containifirst gas) counter current contact, the hydrocarbon component in the hydro carbons enriched gas is absorbed.The rich absorbent that has absorbed hydrocarbon component is recycled returning to external hydrocarbon liquids system, then after the hydrocarbon-containifirst gas mixing of access to plant, enter the adsorption tanks that another is in adsorbed state from the air that is in the state of balancing each other of absorption cat head discharge and the mixed gas (or being called noncondensable gas) of a small amount of hydrocarbon component, after adsorption tanks internal adsorption agent absorption, the tail gas of cleaning enters atmosphere.In the later stage in desorption and regeneration stage, in the adsorption tanks that are in detachment status, inject an amount of air, further stripping goes out a small amount of hydrocarbon component residual on the sorbent material, and sorbent material is thoroughly regenerated.Two adsorption tanks switching single jobs in per approximately 15 minutes under time variable control make the entire operation process continuous.
Although compare with existing other method, absorption method all has a clear superiority at aspects such as exhaust emissions index, plant investment, process costs, but from the angle in market, the plant investment of existing absorption method is still than higher, and the installed capacity of power-equipment is still bigger, and energy consumption is higher.Cause a major reason of the problems referred to above to be, existing absorption method process unit is to mate whole device for recovering oil and gas according to the requirement that can satisfy maximum instantaneous flow and concentration, that is to say, the Design of device principle is, even the air input of hydrocarbon-containifirst gas and inlet gas concentration stably keep maximum instantaneous flow and concentration, device still can satisfy service requirements constantly.We know, in places such as the bigger and concentrated oil depot of light hydrocarbons liquid product filling weight, transhipment station, refinerys, the filling weight of day part usually is quite unbalanced within one day, and the workload of the overwhelming majority concentrates in operation period on daytime and finishes.Even in the operation period by day, be subjected to the influence of various factors, the filling weight fluctuation is also very big, and it is that many tank cars carry out charging operation that a certain period may have several crane positions that fill simultaneously, and another period may not have the tank car charging operation.Hydrocarbon-containifirst gas is produced by filling process, and charging operation amount unbalanced must be caused the unbalanced of device for recovering oil and gas air input.Except that the mass flow discrepancy weighing apparatus, the concentration of hydrocarbon-containifirst gas also fluctuates, same tank car, and the hydrocarbon-containifirst gas concentration that generally fills initial generation is low, and fills concentration height when finishing; Be subjected to the influence of various factors, varying environment condition, different slots bassinet structure, different work mode etc. also can cause the variation of hydrocarbon-containifirst gas concentration.In addition, absorption/desorption the switching cycle of two adsorption tanks of existing absorption method technology generally is about 15 minutes, in adsorption tanks are in 15 fens clock times of desorption manipulation, there are 3～5 fens clock times will be used on the operation sequences such as valve switching, air stripping, pressure recovery.That is to say, will finish vacuum desorption in 10～13 minutes effectual time in the hydrocarbon component of 15 minute period internal adsorption, this just makes the capacity of equipment response of regeneration recovery part increase by 13～25%.Exactly because the existence of above-mentioned factor, the regeneration recovery part of the device for recovering oil and gas of prior art often working ability is very big, is in idle state in the most of the time, utilization ratio of device is not high, the installed capacity of device internally-powered equipment is big, and efficient is low, and energy consumption is higher.
The above-mentioned defective that existing absorption method technology exists has restricted the marketing application that oil gas reclaims project to a great extent; because if taking environmental conservation into consideration social benefit not; investment enterprise is weighed from the economic benefit that reclaims the oil gas generation merely; this project lacks enough magnetisms, thereby this intermediate item helps reducing topsoil, protect the social benefit of environment also can't be embodied.
Goal of the invention
An object of the present invention is to propose a kind of investment of effective reduction absorption method device for recovering oil and gas and the method for operation energy consumption.
Another object of the present invention is the technical process that proposes the absorption method oil gas recovery of a kind of low investment, less energy-consumption.
Summary of the invention
The objective of the invention is by adopting the absorption method Investigation of Petroleum Vapor Recovery Technology of adsorption operation and desorption and regeneration operation at times to realize. The device of this Investigation of Petroleum Vapor Recovery Technology has two adsorption tanks, loading in the adsorption tanks and hydrocarbon component is had affinity and air is not almost being had the solid absorbent of affinity, the total filling amount of two interior adsorbents of adsorption tanks can satisfy the requirement of the hydrocarbon component in whole hydrocarbon-containifirst gases that working day, interior charging operation produced of absorption, and makes the tail gas through discharge after the absorption reach discharge standard. The first adsorption tanks are wherein born the task of absorption the first fishing time hydrocarbon component, and the second adsorption tanks are born the task of absorption the second fishing time hydrocarbon component. Carry out under the steam stripped condition at vacuum and a small amount of air of injection that vavuum pump provides, utilize fully long the first fishing time and the second fishing time, respectively the adsorbent in the second adsorption tanks and the first adsorption tanks is carried out desorption and regeneration, and desorption hydrocarbon component is out reclaimed. By prolonging the time of desorption and regeneration, effectively reduce the scale of regeneration recovery section, reach the purpose that reduces device gross investment and operation energy consumption.
The inventor thinks after absorption method oil gas recovery technique and device are researched and analysed to having now, in the device for recovering oil and gas of prior art, the investment of two adsorption tanks (adsorbent that comprises filling in the tank) only accounts for about 15% of device gross investment usually, all the other most of investments all concentrate on process equipment that the desorption and regeneration of serving adsorbent and hydrocarbon component reclaim the regeneration recovery section of function, instrument, the aspect such as electric, and the main operation energy consumption of device also concentrates on this. Even prior art has two adsorption tanks, also only having all the time one during actual motion is to be in adsorbed state. If with the method for operation by two adsorption tanks of prior art at any time mutually the operator scheme of handover operation (switching once in about 15 minutes) change into an operator scheme of carrying out the desorption and regeneration operation of one-period working day, for adsorption tanks itself, equipment can increase undoubtedly, investment can increase, but the other parts for whole device, because the scale of regeneration recovery section depends primarily on the hydrocarbon component total amount of the desorption and regeneration of wanting and the time of desorption and regeneration operation, needn't be limited by maximum instantaneous flow and the maximum instantaneous concentration of the hydrocarbon-containifirst gas of motion device, device can utilize sufficient the second fishing time and the first fishing time to finish the desorption and regeneration operation, prolonged the time of desorption and regeneration operation, thereby so that except adsorption tanks the scale of all the other nearly all equipment greatly reduce, and load is evenly. The benefit that adopts this method to bring is apparent. The scale that at first accounts for the regeneration recovery section of the main share of device gross investment greatly reduces, and brings the greatly reduction of regeneration recovery section investment, causes whole plant investment to reduce; Secondly, the installed capacity of whole device power-equipment greatly reduces, and on dependence and the impact reduction of outside electric power system, the investment of externally fed system reduces; Moreover, install invalid and the minimizing of poor efficiency activity duration, so that device operation efficiency improves, operation energy consumption reduces; In addition, because the equipment size of regeneration recovery section reduces greatly, it is integrated to install realization easy to manufacture, thereby has reduced the workload of on-the-spot installation, debugging and service, and maintenance cost reduces; Also have, the greatly reduction of regeneration recovery section scale is so that the floor space of whole device also reduces greatly.
Below be major technique, the economic target contrast of device for recovering oil and gas that is used to recycle the hydrocarbon-containifirst gas that produces when oil depot gasoline fills tank car of adopting prior art and adopting the equal scale of two covers of the technology of the present invention, equal recovering effect.
Prior art and the technology of the present invention main economic and technical indices contrast table
| Project | Prior-art devices | The technology of the present invention device |
| Hydrocarbon-containifirst gas maximum instantaneous flow m 3/hr | 500 | 500 |
| The maximum average daily flow m of hydrocarbon-containifirst gas 3/day | 1000 | 1000 |
| 15 minutes hydrocarbon-containifirst gas peak concentration v% | 40 | 40 |
| The maximum average daily concentration v% of hydrocarbon- | 30 | 30 |
| Reclaim hydrocarbon component amount kg/day | 870 | 870 |
| Amounts of activated carbon m in the | 20 | 60 |
| Vacuum pump discharge capacity m 3/hr | 2300 | 210 |
| Poor gasoline flow m
3/ | 55 | 5 |
| Adsorption tanks+gac investment (ten thousand yuan) | 20 | 50 |
| Instrument electricity and other investment (ten thousand yuan) RMB | 110 | 38 |
| Gross investment (ten thousand yuan) RMB | 130 | 88 |
| Total installation of generating capacity kw | 95 | 11 |
| Unit consumption of energy kwh/kg | 0.22 | 0.10 |
By contrast as can be seen, handle 1000m equally
3The hydrocarbon-containifirst gas of/day, the technology of the present invention compared with prior art, gross investment is equivalent to 68%, installed capacity is equivalent to 12%, the energy consumption that reclaims every kg hydrocarbon component is equivalent to 45%.
The present invention for realizing the technical process that above-mentioned oil-gas recovery method proposes is: will be divided into two operation periods a working days, i.e. the first operation period and the second operation period.In the first operation period, first adsorption tanks are in adsorbed state, the hydrocarbon-containifirst gas that filling process produces is introduced into first adsorption tanks of device for recovering oil and gas by pipeline, utilize the solid adsorbent that hydrocarbon component is had avidity that is loading in the adsorption tanks, hydrocarbon component in the hydrocarbon-containifirst gas is adsorbed on the surface of sorbent material, almost do not conform to hydrocarbon component through after the adsorption treatment, the cleaning tail gas that reaches emission standard enters atmosphere.The end of the first operation period enters second charging operation during period, and blocked operation makes first adsorption tanks enter the desorption and regeneration state for the first time, and simultaneously, second adsorption tanks enter adsorbed state.Desorption and regeneration to sorbent material is realized by vacuum desorption and the steam stripped method of air, under the vacuum condition that vacuum pump produces, the most of hydrocarbon component desorption that is adsorbed on the adsorbent surface in first adsorption tanks is got off.The hydro carbons enriched gas that obtains enters the recovery unit after vacuum pump boosts and cools off, recovery vacuum pump boosts and cools off the hydrocarbon liquids that the back generates simultaneously.Reclaiming the unit, the most hydrocarbon component in the hydro carbons enriched gas are recovered, and obtain air and the hydrocarbon component blended noncondensable gas that is not recovered on a small quantity.Above-mentioned noncondensable gas mixed with the hydrocarbon-containifirst gas of this period access to plant introduce second adsorption tanks, when these gases pass when adsorbent bed, hydrocarbon component wherein is adsorbed on the adsorbent surface, and the cleaning tail gas that reaches emission standard enters atmosphere.When the pressure of first adsorption tanks is reduced to setting pressure, in first adsorption tanks, inject an amount of air, sorbent material is carried out stripping, further a small amount of hydrocarbon component desorption residual on the sorbent material is come out.After stripping process was finished, first adsorption tanks recovered normal pressure.Behind the first adsorption tanks desorption and regeneration end of processing, blocked operation for the second time, device transferred for the first operation period to by the second operation period again, and first adsorption tanks return to adsorbed state, and in the early stage of the first operation period, second adsorption tanks are in detachment status.With the process similar sorbent material in second adsorption tanks is carried out desorption and regeneration to the first adsorption tanks desorption and regeneration, and mixes with the hydrocarbon-containifirst gas of access to plant and introduce first adsorption tanks reclaiming the noncondensable gas of discharging the unit in the desorption and regeneration process, make tail gas after the process adsorption treatment reach requirement and discharge.When the pressure in second adsorption tanks is reduced to setting pressure, equally also inject an amount of air, sorbent material is carried out stripping, further a small amount of hydrocarbon component desorption residual on the sorbent material is come out.After the second adsorption tanks desorption and regeneration finishes, recover normal pressure, close down all the other moving equipment and static equipments except that first adsorption tanks.Whole device for recovering oil and gas enters another workaday circulation.
In flow process of the present invention, the quantity of sorbent of two interior fillings of adsorption tanks should satisfy the whole hydrocarbon component that can adsorb in the hydrocarbon-containifirst gas that filling process gives off in whole working days, and can guarantee that hydrocarbon-containifirst gas reaches emission standard through the tail gas of discharging after the adsorbents adsorb.Wherein the quantity of sorbent of filling satisfies the requirement that the hydrocarbon-containifirst gas of the first operation period of adsorption treatment access to plant and the first operation period reclaim the noncondensable gas of discharging the unit at least in first adsorption tanks, and the quantity of sorbent of filling satisfies the requirement that the hydrocarbon-containifirst gas of the absorption second operation period access to plant and the second operation period reclaim the noncondensable gas of discharging the unit at least in second adsorption tanks.The loadings of the size of first, second adsorption tanks and jar internal adsorption agent depends primarily on and receives separately and the hydrocarbon component amount of adsorption treatment and the saturated adsorptive power of the sorbent material that is adopted.The hydrocarbon component amount of reception and adsorption treatment is big more, and required quantity of sorbent is also just big more; The saturated adsorptive power of sorbent material is big more, and the required quantity of sorbent of hydrocarbon component of absorption same amount is just more little.
First adsorption tanks need to determine according to user's particular case at the hydrocarbon-containifirst gas volume of the second charging operation period adsorption treatment at the hydrocarbon-containifirst gas volume and second adsorption tanks of the first operation period adsorption treatment.Generally, can produce the operation period (such as daytime) of most of hydrocarbon-containifirst gas as the first operation period with comparing the concentrated area in whole working days, the hydrocarbon-containifirst gas that produces in this period is by the first adsorption tanks adsorption treatment, and such first adsorption tanks are bigger adsorption tanks that loading relatively large sorbent material; And all the other produce a small amount of hydrocarbon-containifirst gas in addition operation period (such as night) of not having hydrocarbon-containifirst gas as the second operation period, the hydrocarbon-containifirst gas that produces in this period is by the second adsorption tanks adsorption treatment, and second adsorption tanks are exactly less adsorption tanks that loading a small amount of sorbent material so.
The sorbent material that uses in the adsorption tanks can be various hydrocarbon component is had preferably avidity and air is not almost had avidity, and solid adsorbent with good vacuum desorption performance, from the contrast of combined factors such as use properties and price, gac is the ideal sorbent material.
For the first time the moment of blocked operation, promptly the first operation period switched to the moment of the second operation period, was an important parameters, and two adsorption tanks internal adsorption agent loadings what not only affect, and also affected the scale of device for recovering oil and gas regeneration recovery part.In general, after for the first time the moment of blocked operation preferably is selected in the charging operation of relatively concentrating working days and finishes, enters the charging operation of comparison rareness, and satisfied before the workaday concentrated charging operation of the next one is arrived, there is time enough to finish the requirement that the desorption and regeneration of first adsorption tanks is operated as the second operation period.For the first time the moment of blocked operation may be with different user's conditions and different seasonal variation and difference.During practical application, blocked operation can switch by setting constantly in sequence of control for the first time; Or switch in conjunction with setting constantly according to measuring parameter (as the flow and the concentration that enter the hydrocarbon-containifirst gas of first adsorption tanks, first adsorption tanks are discharged the hydrocarbon component concentration of tail gas etc.); Also can manual operation switch.
For the first time blocked operation and timed interval between the blocked operation for the second time just the length of the time of the second operation period depend primarily on the scale of the hydrocarbon component amount of the first operation period first adsorption tanks internal adsorption and the recovery part of regenerating.The scale of said regeneration recovery part refers to the processing power of regeneration recovery part in the unit time.The hydrocarbon component amount of the first adsorption tanks internal adsorption is big more, and the scale of regeneration recovery part is more little, and the time of the second operation period is just long more; Otherwise the hydrocarbon component amount in first adsorption tanks is more little, and the scale of regeneration recovery part is big more, and the time of the second operation period is just short more.With the first time blocked operation different, for the second time blocked operation is behind the desorption and regeneration end of processing of first adsorption tanks, is realized automatically by time variable control.
The desorption and regeneration of the sorbent material in first adsorption tanks and second adsorption tanks realizes that under vacuum condition setting pressure is the important factor of decision desorption and regeneration effect.At the initial stage in desorption and regeneration stage, the pressure in the adsorption tanks is normal pressure, along with the carrying out of desorption and regeneration process, the jar internal pressure reduces gradually, hydrocarbon component also gradually from the sorbent material desorption come out, until near or when reaching setting pressure, most hydrocarbon component all from the sorbent material desorption come out.Theoretically, setting pressure is low more, and the hydrocarbon component desorption on the sorbent material must be thorough more, switch to adsorbed state after, just low more through hydrocarbon component content in the tail gas that gives off of absorption.But, the restriction of sealing liquid saturation vapour pressure because the minimum suction pressure that the liquid-ring vacuum pump that generally uses can reach is subjected to circulating, when the very low setting pressure of needs, need the vacuum pump or the series connection vacuum pump of other pattern to realize, this will increase investment and process cost, therefore, generally, people determine setting pressure according to the exhaust emissions index that device for recovering oil and gas will satisfy.Majority state and geographic exhaust emissions index are not to be higher than 10～35mg/l in the world at present, when adopting gac as sorbent material, setting pressure is generally 40～110mmHg (absolute pressure), and reach when not being higher than 0.15mh/l when the exhaust emissions index request, setting pressure is what for to reaching 1mmHg (absolute pressure).
The hydrocarbon component that reclaims unitary major function and be in the hydro carbons enriched gas after vacuum pump outlet is boosted reclaims.The specific implementation method can adopt absorption process technology, or condensation method technology.
Absorption process technology be used for exactly from install external system, with hydrocarbon-containifirst gas in the same or analogous hydrocarbon liquids of hydrocarbon component character (normally adopting the identical hydrocarbon liquids of liquid property) with generation gas hydrocarbon component make absorption agent, in the absorption tower with hydro carbons enriched gas counter current contact, in this process, most of hydrocarbon component in the hydro carbons enriched gas is absorbed agent and absorbs, discharge from absorbing cat head through the noncondensable gas that contains a small amount of hydrocarbon component after absorbing, the rich absorbent that has absorbed hydrocarbon component is then sent back to external system.Comparatively speaking, absorption process technology is fairly simple, and investment and running cost are also lower, and the hydrocarbon component of recovery is directly mixed with absorption agent, and the hydrocarbon liquids that can save recovery stores specially with blended and bothers.
The ultimate principle of condensation method technology is by reducing condensing temperature or improving condensing pressure, the hydrocarbon component in the hydro carbons enriched gas to be condensed into hydrocarbon liquids.According to the principle that balances each other, the hydrocarbon component boiling point in the hydro carbons enriched gas is low more, and concentration is low more, and required condensing temperature is just low more, and condensing pressure is high more.For the hydro carbons enriched gas of definite composition and concentration, condensing temperature is low more, and then required condensing pressure is also low more; Otherwise condensing temperature is high more, and then required condensing pressure is also high more.Therefore can be cryogenic condensation by the condensing temperature that reduces hydro carbons enriched gas condensation process, or to improve condensing pressure be compression condensation, or to reduce condensing temperature simultaneously and improve condensing pressure be the purpose that the low temperature compression condensation realizes hydrocarbon component is condensed into liquid.Calculate according to the processing simulation that the inventor did, generally, reclaiming unitary condensing temperature should be at-40 ℃～normal temperature, and condensing pressure should be in 0～2.0Mpa (gauge pressure), the too high or condensing pressure of condensing temperature cross low can cause hydrocarbon component reclaim the unit can not be by abundant condensation; And condensing temperature is crossed low or the too high meeting of condensing pressure causes the excessive facility investment and the increase of running cost.Compare with the existing condensation method oil gas recovery technology of directly hydrocarbon-containifirst gas being carried out the atmospheric low-temperature condensation, the present invention adopts condensation process more rationally feasible in the recovery unit.At first, the gas that comes out from the adsorption tanks desorption is the hydro carbons enriched gas, the mean concns of hydrocarbon component wherein reaches about 90%, far above 35% left and right sides mean concns of hydrocarbon-containifirst gas, and the obvious condensation hydro carbons enriched gas condensing condition milder more required than condensation hydrocarbon-containifirst gas; Moreover, compare with the hydrocarbon-containifirst gas of access to plant, enter the maximum instantaneous flow that reclaims unitary hydro carbons enriched gas among the present invention and reduce greatly, flow and concentration are more even, and required refrigeration load is also just smaller; In addition, after also will being in the adsorption treatment of adsorption tanks of adsorbed state through another, the noncondensable gas of discharging the unit just enters atmosphere from reclaiming among the present invention, like this, the concentration of the hydrocarbon component of the noncondensable gas of discharging from the recovery unit needn't be limited by the restriction of emission standard, can allow highlyer relatively, this also makes condensing condition more gentle.Reclaim the unit and adopt condensation process to want accurately to understand and grasp the hydrocarbon liquids amount that is reclaimed, or employing absorption process technology provides the absorption agent inconvenient user of circulating that a kind of selection is provided by external system for those.
In order to strengthen the desorption and regeneration effect, in the later stage in adsorption tanks desorption stage, when just the pressure in the adsorption tanks reaches setting pressure, can in adsorption tanks, inject an amount of air, utilize the air that injects further to reduce a jar interior oil gas dividing potential drop, by the stripping effect of air, can make the hydrocarbon component that remains on the sorbent material obtain desorption more completely.Outside the deacration, also can make stripping gas with other rare gas element such as nitrogen etc.
Though technical process of the present invention is particularly suitable for reclaiming charging operation amount and the bigger light hydrocarbons liquid product of fluctuation of concentration, hydrocarbon component in the hydrocarbon-containifirst gas that produces during as gasoline, kerosene, crude oil, solvent oil, benzene-type products etc., but be suitable for reclaiming the hydrocarbon component in the bigger hydrocarbon-containifirst gas of processing, the flow that produces when storing hydrocarbon liquids and fluctuation of concentration too, or the flow that gives off when processing, storing, fill other volatile organic matter liquid and fluctuation of concentration bigger contain volatile organic matter component in the volatile organic matter gas.
Description of drawings
Figure the-1st, schematic flow sheet of the present invention.
Figure the-2nd reclaims the schematic flow sheet that the unit adopts absorption process technology.
Figure the-3rd reclaims the schematic flow sheet that the unit adopts condensation method technology.
Figure-4 is device for recovering oil and gas operation on working days handoff procedure synoptic diagram.
Embodiment
In the flow process shown in the figure-1, first adsorption tanks (1) and second adsorption tanks (6) are an adsorption devices that solid adsorbent (gac) bed (9) and bed (10) are being loaded in two inside, source line (30) one ends that hydrocarbon-containifirst gas enters device for recovering oil and gas connect emission source (not drawing among the figure), and the other end is communicated with the inlet of first adsorption tanks (1) and second adsorption tanks (6) by pipeline (31) and pipeline (44) respectively.One end of pipeline (32) is communicated with the outlet of first adsorption tanks (1), and the other end is communicated with atmosphere.One end of pipeline (45) is communicated with the outlet of second adsorption tanks (6), and the other end is communicated with atmosphere.On source line (31), pipeline (44) and the outlet line (32) of adsorption tanks, pipeline (45), switch-valve (20), switch-valve (24) and switch-valve (21), switch-valve (25) are installed respectively.Pipeline (34) and pipeline (47) are respectively that the air of first adsorption tanks (1) and second adsorption tanks (6) injects line, the one end directly is communicated with atmosphere, the other end is connecting pipeline (32) and pipeline (45) respectively, and switch-valve (22) and switch-valve (26) are being set respectively on pipeline (34) and pipeline (47).The vacuum pump (2) that is used to provide vacuum condition is a liquid-ring vacuum pump, and the sealing liquid that liquid-ring vacuum pump uses is water and ethylene glycol mixtures.Why adopt liquid-ring vacuum pump, not only, the more important thing is its compression process near mechanical frictional sparking can taking place in isothermal compression and the operational process, so safety in operation is good because its vacuum performance is better, cheap.When the desorption and regeneration required pressure is very low, can before liquid-ring vacuum pump, increase a vacuum gooster pump (not drawing among the figure).Certainly, the vacuum pump of other form can satisfy the technology service requirements too.Vacuum pump (2) has an inlet, an outlet and a sealing liquid return port.One end of vacuum pump inlet pipeline (36) is connected with the inlet of vacuum pump (2), the other end is communicated with the first adsorption tanks source line (31) and the second adsorption tanks source line (44) by pipeline (35) and pipeline (48) respectively, is respectively equipped with switch-valve (23) and switch-valve (27) on pipeline (35) and the pipeline (48).One end of vacuum pump outlet pipeline (37) links to each other with vacuum pump outlet, and the other end is communicated with the top of first separator (3).First separator (3) is a triphase separator, and the boost hydrocarbon liquids and the round-robin sealing liquid that may generate in the process of hydro carbons enriched gas, the vacuum pump after vacuum pump can being boosted separated.The hydro carbons enriched gas pipeline (38) at first separator (3) top is communicated with the recovery unit of frame of broken lines (100) representative, is communicated with motion device hydrocarbon-containifirst gas tube (30) by pipeline (43) through reclaiming the noncondensable gas of discharging after the unit recovery hydrocarbon component.In first separator (3), hydrocarbon liquids and sealing liquid are two-layer up and down because of difference in specific gravity is divided into, and what be in the upper strata is hydrocarbon liquids (7), and what be in lower floor is sealing liquid (8).The pipeline (42) that is connected separator (3) middle part is the vent line of hydrocarbon liquids, by this pipeline can with the hydrocarbon liquids that obtains at first separator (3) from press or boost with pump (not drawing among the figure) after enter the external system storage tank, or draining into the recovery unit, the hydrocarbon liquids that obtains with the recovery unit mixes mutually.The liquid (8) of first separator (3) bottom is the sealing liquid of vacuum pump (2), the inlet end of sealing liquid pump (4) is communicated with first separator (3) bottom by pipeline (39), the outlet of sealing liquid pump (4) links to each other with water cooler (5) inlet by pipeline (40), and the outlet of water cooler (5) links to each other with vacuum pump (2) sealing liquid return port by pipeline (41).
What frame of broken lines (100) was represented is to reclaim the unit, according to different conditions and requirement, reclaims the unit and can adopt absorption process technology or condensation method technology.
Figure the-2nd reclaims the schematic flow sheet that the unit adopts absorption process technology.Loading the filler or the column plate (51) that are suitable for mass transfer in the absorption tower (50).Be connected the middle part of absorption tower (50) from the pipeline (38) at first separator (3) top, overhead line (43) is through the noncondensable gas outlet line after absorbing, the pipeline (53) that is connected tower top is the absorption agent source line, its other end link to each other with the external absorbent system (not drawing among the figure).Absorption agent pump (52) is the overboard pump that has absorbed the rich absorbent after the hydrocarbon component, and the inlet of absorption agent pump (52) is communicated with at the bottom of the tower by pipeline (54), and its outlet is connected to external absorbent system (not drawing among the figure) by pipeline (55).
Absorption tower (50) and first separator (3) can the split settings (as figure-1 and scheme shown in-2), also can be combined into one, be the top that absorption tower (50) is seated first separator (3), at this moment the rich absorbent at the bottom of the tower directly mixes the back discharge with the hydrocarbon liquids that vacuum pump outlet condenses.
Figure the-3rd reclaims the unit and adopts condensation method technology to reclaim the schematic flow sheet of hydrocarbon component.In this flow process, hydrocarbon component gas is condensed into liquid in condenser (60), and the required cryogenic cooling medium of condensation process is provided by special unit cooler (not drawing among the figure) or other external source.When condensing pressure is not too high, directly condensation under the top hole pressure of vacuum pump (2), owing to be subjected to the restriction of vacuum pump self-condition, generally condensing pressure is not higher than 0.2Mpa (gauge pressure); When the higher condensing pressure of needs, special compressor (not drawing among the figure) can be set before condenser, by boosting of compressor, make hydrocarbon component under higher pressure, be condensed into liquid.Hydro carbons enriched gas pipeline (38) from first separator (3) top links to each other with the inlet of condenser (60), condensator outlet pipeline (63) is connected the middle part of second separator (61), the pipeline (43) that is connected second separator (61) top is the noncondensable gas outlet line, condensing pressure can be controlled (when condensing pressure is barometric point, not establishing this control valve) by the self-forced type pressure controlled valve (63) that is located on this pipeline.Carrying device after the hydrocarbon liquids that generates in the condensation process can boost by hydrocarbon liquids pump (62), the inlet of hydrocarbon liquids pump (62) is communicated with second separator (61) bottom by pipeline (65), and its outlet is communicated with the hydrocarbon liquids storage tank (not drawing among the figure) of external system by pipeline (66).Need to prove, reclaim the unit and adopt the specific implementation method of condensation method technology can have multiple.Can adopt above-mentioned indirect condensing technology, also can adopt, the hydro carbons enriched gas be carried out the direct condensation process etc. of direct absorption condensation with being cooled to cryogenic hydrocarbon liquids again by the cooling hydrocarbon liquids.For the engineering technical personnel that are familiar with this professional domain,, be not difficult to propose the improvement project of numerous concrete technology according to spirit of the present invention.
Figure the-4th, oil gas reclaimer operation process switching on the working days synoptic diagram of an embodiment who draws for ease of understanding work flow of the present invention.Transverse axis among the figure is represented the time coordinate axle, is first adsorption tanks above in the running status of the first operation period and the second operation period, is the running statuses of second adsorption tanks in the first operation period and the second operation period below.Article 3, vertically thick long and short dash line was divided into the first operation period and two periods of the second operation period in workaday 24 hours with one, and wherein, the vertically thick long and short dash line of intermediary represent the moment of the blocked operation first time.Laterally heavy line represents that adsorption tanks are in adsorbed state, and laterally thick dashed line represents that adsorption tanks are in the desorption and regeneration state, and vertically the moment of the second adsorption tanks desorption and regeneration end of processing is represented in the choice refreshments setting-out.
Operation situation below in conjunction with figure-1, figure-2 and-4 pairs of whole technological processs of figure describes.
The first operation period after second adsorption tanks (6) desorption and regeneration finishes (5 up to period of 20 o'clock among the figure-4); whole device is except that open switch-valve (20) and (21); all the other valves are all closed; install all moving equipment and all be in stopped status; the hydrocarbon-containifirst gas that filling process produces enters first adsorption tanks (1) through pipeline (30), switch-valve (20) and pipeline (31); sorbent material (9) in the adsorption tanks absorbs hydrocarbon component wherein, and the cleaning tail gas of hydrocarbon-containifirst component then enters atmosphere by pipeline (32) and switch-valve (21) hardly.
When first adsorption tanks (1) move to 20 constantly under adsorbed state, arrive the moment of blocked operation for the first time, at this moment, open switch-valve (23), (24), (25), all the other valves are all closed, and first adsorption tanks (1) enter the desorption and regeneration state, and second adsorption tanks (6) enter adsorbed state.Adopt absorption process (shown in figure-2) if reclaim the unit, at this moment introduce absorption agent from the external absorbent system, and start absorption agent pump (52), absorption agent forms circulation; Start sealing liquid pump (4), the sealing liquid circulation; Start vacuum pump (2), the desorption and regeneration of first adsorption tanks (1) begins.Along with constantly being inhaled into of vacuum pump (2) inlet gas, pressure in first adsorption tanks (1) reduces gradually, the first operation period be adsorbed on the sorbent material hydrocarbon component gradually desorption come out, mix forming the hydro carbons enriched gas along pipeline (35), enter vacuum pump (2) through switch-valve (23) and pipeline (36) with the hydrocarbon-containifirst gas that retains in the jar.Enter the circulation sealing liquid of also having of vacuum pump (2) simultaneously with the hydro carbons enriched gas from pipeline (41).After vacuum pump (2) boosted, the small quantities of hydrocarbon class I liquid I that may generate after hydro carbons enriched gas and the compression mixed the gas-liquid mixture that forms and enters first separator (3) by pipeline (37) with sealing liquid.After entering first separator (3), gas-liquid mixture separates, and gas enters the recovery unit from the top by pipeline (38).Liquid phase may have two-phase, and one is the round-robin sealing liquid mutually, and another is the hydrocarbon liquids that hydrocarbon component condensation wherein heavier after the hydro carbons enriched gas boosts forms mutually.Because there is significant difference in specific gravity and immiscible in two kinds of liquid, two-phase AUTOMATIC ZONING in separator, the less hydrocarbon liquids (7) of proportion is in the upper strata, and the sealing liquid that proportion is bigger (8) is in lower floor.The sealing liquid of lower floor is extracted out by pipeline (39), after sealing liquid pump (4) boosts, enters water cooler (5) cooling by pipeline (40), and cooling forms circulation after pipeline (41) enters vacuum pump.The methods for cooling of sealing liquid water cooler (5) can adopt air cooling or recirculated water cooling or processing medium cooling, when the recovery unit of device adopts absorption process technology, preferably adopts absorption agent to make heat-eliminating medium.The hydrocarbon liquids (7) on the interior upper strata of first separator (3) press certainly by pipeline (42) or boost with pump (not drawing among the figure) after enter the external system storage tank, or drain into and reclaim the unit and mix mutually with the hydrocarbon liquids that the recovery unit obtains.
In reclaiming unitary absorption tower (50), go up counter current contact from absorption agent (as the gasoline) from top to down that cat head enters in the tower at filler (51) from bottom to up with by pipeline (53) by the hydro carbons enriched gas that pipeline (38) enters in the tower from the tower middle part, in this process, most of hydrocarbon component is absorbed the agent absorption in the hydro carbons enriched gas, the rich absorbent that has absorbed hydrocarbon component is finally extracted out at the bottom of tower, by pipeline (54), and after absorption agent pump (52) boosts, under the control of base level control loop (not drawing among the figure), turn back in the outside absorber systems through pipeline (55) circulation.Air in the unabsorbed hydro carbons enriched gas and be the hydrocarbon component that balances each other with absorption agent and mix the noncondensable gas that forms and then discharge from cat head, after mixing pipeline (43) and this moment by the hydrocarbon-containifirst gas of pipeline (30) access to plant, enter second adsorption tanks (6) that are in adsorbed state through switch-valve (24) and pipeline (44), sorbent material (10) in the adsorption tanks absorbs the hydrocarbon component in the mixed gas equally, through the gas after the adsorption treatment is the cleaning tail gas that does not almost conform to hydrocarbon component too, and this gas finally enters atmosphere by pipeline (45) and switch-valve (25).
Carrying out along with first adsorption tanks (1) desorption and regeneration process, the adsorption tanks internal pressure reduces gradually, increasing hydrocarbon component desorption from the sorbent material goes out to adopt, and when the pressure in adsorption tanks reached the setting pressure of 70mmHg, the hydrocarbon component of the overwhelming majority was all come out by desorption and is recovered.More thorough for adsorbent reactivation is got, inject a little air and carry out stripping this moment.Open switch-valve (22), air enters first adsorption tanks (1) via pipeline (34), switch-valve (22), and the dividing potential drop of the hydrocarbon component in the entering of air reduced jar makes hydrocarbon component residual on the sorbent material by thorough desorption, and sorbent material obtains holomorphosis.
After injection air program is finished, first adsorption tanks (1) are recovered normal pressure.Close switch-valve (23), (22), slowly open switch-valve (21), air enters first adsorption tanks (1) through switch-valve (21) and pipeline (32), makes the adsorption tanks internal pressure recover normal pressure gradually.Recover in the non-pressurized process at first adsorption tanks (1), vacuum pump (2) can out of service or import and export gas circulation.
Behind the pressure recovery normal pressure in first adsorption tanks (1), beginning is blocked operation (among the figure-4 is 4 o'clock) for the second time, and first adsorption tanks (1) return to adsorbed state, and second adsorption tanks (6) enter the desorption and regeneration state.At this moment, open switch-valve (20), (21), (27), all the other valve closess, vacuum pump (2) is opened, from the hydro carbons enriched gas of second adsorption tanks (6) through pipeline (48), switch-valve (27)) and pipeline (36) enter vacuum pump (2), identical with the aforesaid removal process that is experienced from the hydro carbons enriched gas of first adsorption tanks (1) afterwards, the most of hydrocarbon component in the hydro carbons enriched gas is recovered down in the recovery unit.Different is, leave reclaim unitary noncondensable gas and discharge via pipeline (43) after, mix after switch-valve (20) and pipeline (31) enter first adsorption tanks (1) with hydrocarbon-containifirst gas, by entering atmosphere after first adsorption tanks (1) adsorption treatment by pipeline (30) access to plant.Equally, when the pressure in second adsorption tanks (6) reaches the setting pressure of 70mmHg, open switch-valve (26), allow a spot of air enter second adsorption tanks (6), the sorbent material (10) in second adsorption tanks (6) is thoroughly regenerated via pipeline (47), switch-valve (26).Afterwards, close down all moving equipment, make back adsorption tanks (6) recovery normal pressure, last, close all valves except that switch-valve (20) and (21), another workaday circulation of device beginning (scheme in-4 this moment is) at 5 o'clock.Because it is fewer to enter the hydrocarbon component amount of second adsorption tanks (6) in the second operation period, therefore, required time of the desorption and regeneration of second adsorption tanks (6) is far fewer than the required time of desorption and regeneration of first adsorption tanks (1).
When device recovery unit adopted the condensation method technology of scheming shown in-3, except reclaiming the unit, the device numbering of device rest part was identical with figure-1 with principle of work, repeats no more herein.According to the technical process shown in the figure-3, the hydro carbons enriched gas of discharging from first separator (3) top is when condensing pressure is not too high, directly enter condenser (60) through pipeline (38), when condensing pressure when higher, after compressed machine (not drawing among the figure) boosts, enter condenser (60).In condenser (60), the hydro carbons enriched gas is cooled off by the refrigeration filling condensation, and hydrocarbon component wherein is condensed into hydrocarbon liquids, leaves the hydrocarbon liquids of condenser (60) and the gas-liquid mixture of noncondensable gas and enters second separator (61) through pipeline (64).Afterwards, gas-liquid separation in second separator (61), the noncondensable gas of separating is discharged from the pipeline (43) that is located at the top, condensing pressure is by self-forced type pressure controlled valve (63) control automatically, when the unitary working pressure of recovery is higher than set(ting)value, control valve (63) is opened greatly, otherwise control valve (63) turns down.The hydrocarbon liquids that second separator (61) bottom obtains is through pipeline (65), after boosting by hydrocarbon liquids pump (62), under the control of liquid level control loop (not drawing among the figure) through pipeline (66) carrying device.
Need to prove that whole device for recovering oil and gas is an organic whole, the operating parameters that the operation of above-mentioned technological process is all recorded by industrial control computer or PLC basis is finished automatically according to predefined program.
Claims (10)
1. method that from hydrocarbon-containifirst gas, reclaims hydrocarbon component, it is characterized in that: two adsorption tanks are arranged, loading in the adsorption tanks and hydrocarbon component is had avidity and air is not almost being had the solid adsorbent of avidity, the total filling amount of two adsorption tanks internal adsorption agent can satisfy the requirement of the hydrocarbon component in whole hydrocarbon-containifirst gases that working days, interior filling process produced of absorption, and make the tail gas of discharging reach emission standard through the absorption back, first adsorption tanks are wherein born the task of the absorption first operation period hydrocarbon component, second adsorption tanks are born the task of the absorption second operation period hydrocarbon component, carry out under the steam stripped condition at vacuum and injection little air that vacuum pump provides, utilize the fully long first operation period and the second operation period, respectively the sorbent material in second adsorption tanks and first adsorption tanks is carried out desorption and regeneration, and the hydrocarbon component that desorption comes out reclaimed, by prolonging the time of desorption and regeneration, effectively reduce the scale of regeneration recovery part, reach the purpose that reduces device gross investment and operation energy consumption; Its technical process mainly comprises following steps:
A) in the first operation period, first adsorption tanks are in adsorbed state, the hydrocarbon-containifirst gas that filling process produces is introduced into first adsorption tanks of device for recovering oil and gas by pipeline, utilize hydrocarbon component is had avidity and air almost not being had the solid adsorbent of avidity of loading in the adsorption tanks, hydrocarbon component in the hydrocarbon-containifirst gas is adsorbed on the surface of sorbent material, through hydrocarbon-containifirst component hardly after the adsorption treatment, the cleaning tail gas that reaches emission standard enters atmosphere;
B) blocked operation for the first time, device entered for the second operation period by the first operation period, and first adsorption tanks enter the desorption and regeneration state, and simultaneously, second adsorption tanks enter adsorbed state;
C) under the vacuum condition that vacuum pump produces, the most of hydrocarbon component desorption that is adsorbed on the adsorption tanks internal adsorption agent surface that is in the desorption and regeneration state is got off, obtain the hydro carbons enriched gas;
D) the hydro carbons enriched gas that obtains of step c) enters the recovery unit after vacuum pump boosts and cools off, and the hydrocarbon liquids of generation is recovered through vacuum pump boosts and cools off after simultaneously;
E) reclaiming the unit, the most hydrocarbon component in the hydro carbons enriched gas are recovered, and obtain air and the hydrocarbon component blended noncondensable gas that is not recovered on a small quantity simultaneously;
F) noncondensable gas that step e) is obtained mixes introducing second adsorption tanks with the hydrocarbon-containifirst gas of the second operation period access to plant, when these gases pass when adsorbent bed, hydrocarbon component wherein is adsorbed on the adsorbent surface, and the cleaning tail gas that reaches emission standard enters atmosphere;
G) when the pressure of first adsorption tanks is reduced to setting pressure, in first adsorption tanks, inject an amount of air, sorbent material is carried out stripping, further a small amount of hydrocarbon component desorption residual on the sorbent material is come out;
H) first adsorption tanks recover normal pressure;
I) blocked operation for the second time, device transferred for the first operation period to by the second operation period, and first adsorption tanks return to adsorbed state, and simultaneously, second adsorption tanks enter the desorption and regeneration state;
J) performing step c successively) to e);
K) with step j) noncondensable gas that obtains mixes with the hydrocarbon-containifirst gas of this period access to plant and introduces first adsorption tanks, when these gases pass when adsorbent bed, hydrocarbon component wherein is adsorbed on the adsorbent surface, and the cleaning tail gas that reaches emission standard enters atmosphere;
L) when the pressure in second adsorption tanks is reduced to setting pressure, inject an amount of air, sorbent material is carried out stripping, further a small amount of hydrocarbon component desorption residual on the sorbent material is come out;
M) second adsorption tanks recover normal pressure;
N) be in the adsorbed state except that first adsorption tanks, close down all the other all moving equipment and static equipments, enter another workaday circulation.
2. processing method according to claim 1 and flow process, it is characterized in that: the quantity of sorbent of filling satisfies the requirement that the hydrocarbon-containifirst gas of the first operation period of adsorption treatment access to plant and the first operation period reclaim the noncondensable gas of discharging the unit at least in first adsorption tanks, and the quantity of sorbent of filling satisfies the requirement that the hydrocarbon-containifirst gas of the second operation period of adsorption treatment access to plant and the second operation period reclaim the noncondensable gas of discharging the unit at least in second adsorption tanks.
3. processing method according to claim 1 and flow process, it is characterized in that: relatively concentrated area operation period of producing most of hydrocarbon-containifirst gas was the first operation period in working days, thereby first adsorption tanks are bigger adsorption tanks that loading relatively large sorbent material, and the operation period that produces all the other a small amount of hydrocarbon-containifirst gases was the second operation period, thereby second adsorption tanks are less adsorption tanks that loading than a small amount of sorbent material.
4. according to claim 1,2 and 3 described processing method and flow processs, it is characterized in that: the solid adsorbent of filling is a gac in first adsorption tanks and second adsorption tanks.
5. technical process according to claim 1 is characterized in that: blocked operation is realized by set switching instant in sequence of control said first time in the step b).
6. technical process according to claim 1 is characterized in that: blocked operation is realized in conjunction with setting switching instant according to measuring parameter said first time in the step b).
7. technical process according to claim 1 is characterized in that: blocked operation is operated by manual switchover and is realized said first time in the step b).
8. technical process according to claim 1 is characterized in that: step g) and l) in said setting pressure be 1～110mmHg (absolute pressure).
9. technical process according to claim 1 is characterized in that: said recovery unit adopts absorption process technology in the step e).
10. technical process according to claim 1 is characterized in that: said recovery unit adopts condensation method technology in the step e).
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101357291B (en) * | 2008-09-27 | 2011-04-20 | 北京信诺海博石化科技发展有限公司 | Treatment technique of polypropylene tail-gas generated by continuous-method polypropylene device |
| CN101385936B (en) * | 2008-10-14 | 2011-06-08 | 北京信诺海博石化科技发展有限公司 | Pressure swing adsorption technique for treating fixed gas of bulk polypropylene device |
| CN102921270A (en) * | 2012-10-31 | 2013-02-13 | 中国石油化工股份有限公司 | Method for oil gas or volatile gas desorption of adsorbent applied to oil gas recovery |
| CN105060255A (en) * | 2015-08-14 | 2015-11-18 | 河北美邦工程科技股份有限公司 | Method for recycling and treating heavy aromatics in oxidized tail gas obtained after oxidation of hydrogenated liquid in technology for producing hydrogen peroxide with anthraquinones process |
| CN112494993A (en) * | 2020-12-28 | 2021-03-16 | 大连福佳·大化石油化工有限公司 | Adsorption tower stripping system and stripping method thereof |
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- 2004-09-18 CN CN 200410079995 patent/CN1749360A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101357291B (en) * | 2008-09-27 | 2011-04-20 | 北京信诺海博石化科技发展有限公司 | Treatment technique of polypropylene tail-gas generated by continuous-method polypropylene device |
| CN101385936B (en) * | 2008-10-14 | 2011-06-08 | 北京信诺海博石化科技发展有限公司 | Pressure swing adsorption technique for treating fixed gas of bulk polypropylene device |
| CN102921270A (en) * | 2012-10-31 | 2013-02-13 | 中国石油化工股份有限公司 | Method for oil gas or volatile gas desorption of adsorbent applied to oil gas recovery |
| CN102921270B (en) * | 2012-10-31 | 2015-09-23 | 中国石油化工股份有限公司 | The petroleum vapor recovery method of adsorbent desorption oil gas or escaping gas |
| CN105060255A (en) * | 2015-08-14 | 2015-11-18 | 河北美邦工程科技股份有限公司 | Method for recycling and treating heavy aromatics in oxidized tail gas obtained after oxidation of hydrogenated liquid in technology for producing hydrogen peroxide with anthraquinones process |
| CN112494993A (en) * | 2020-12-28 | 2021-03-16 | 大连福佳·大化石油化工有限公司 | Adsorption tower stripping system and stripping method thereof |
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