CN100584431C - Method for treating and recovering gaseous hydrocarbon - Google Patents
Method for treating and recovering gaseous hydrocarbon Download PDFInfo
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- CN100584431C CN100584431C CN200710108900A CN200710108900A CN100584431C CN 100584431 C CN100584431 C CN 100584431C CN 200710108900 A CN200710108900 A CN 200710108900A CN 200710108900 A CN200710108900 A CN 200710108900A CN 100584431 C CN100584431 C CN 100584431C
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Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B67—OPENING, CLOSING OR CLEANING BOTTLES, JARS OR SIMILAR CONTAINERS; LIQUID HANDLING
- B67D—DISPENSING, DELIVERING OR TRANSFERRING LIQUIDS, NOT OTHERWISE PROVIDED FOR
- B67D7/00—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes
- B67D7/04—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes for transferring fuels, lubricants or mixed fuels and lubricants
- B67D7/0476—Vapour recovery systems
- B67D7/0478—Vapour recovery systems constructional features or components
- B67D7/049—Vapour recovery methods, e.g. condensing the vapour
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B67—OPENING, CLOSING OR CLEANING BOTTLES, JARS OR SIMILAR CONTAINERS; LIQUID HANDLING
- B67D—DISPENSING, DELIVERING OR TRANSFERRING LIQUIDS, NOT OTHERWISE PROVIDED FOR
- B67D7/00—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes
- B67D7/04—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes for transferring fuels, lubricants or mixed fuels and lubricants
- B67D7/0476—Vapour recovery systems
- B67D7/0478—Vapour recovery systems constructional features or components
- B67D7/0488—Means for preventing the formation of condensation on, or for removing condensation from, vapour recovery lines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B67—OPENING, CLOSING OR CLEANING BOTTLES, JARS OR SIMILAR CONTAINERS; LIQUID HANDLING
- B67D—DISPENSING, DELIVERING OR TRANSFERRING LIQUIDS, NOT OTHERWISE PROVIDED FOR
- B67D7/00—Apparatus or devices for transferring liquids from bulk storage containers or reservoirs into vehicles or into portable containers, e.g. for retail sale purposes
- B67D7/06—Details or accessories
- B67D7/42—Filling nozzles
- B67D7/54—Filling nozzles with means for preventing escape of liquid or vapour or for recovering escaped liquid or vapour
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Loading And Unloading Of Fuel Tanks Or Ships (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
The invention provides a small-sized and cheap gaseous hydrocarbon treating and recovering device and method for preventing adsorbent poisoning due to the influence of moisture contained in gasoline steam, the method is characterized in that the device is provided with a means for cooling the adsorption/desorption device in the adsorption/desorption device respectively provided with at least one of an adsorption tower and a desorption tower, the adsorption/desorption device is used as adsorbent, single silica gel or synthetic zeolite with pore diameter of 4-100 angstrom or mixture thereof is used for adsorption/desorption, furthermore, a part of outlet gas of the adsorption tower is sent to the desorption tower, and the gas during desorption is used as purified gas.
Description
Technical field
The present invention relates to be released to processing, retracting device and the method for gas-state hydrocarbon contained in the gas of atmosphere, particularly relate to the device and the method for the gasoline vapor that leaks when being used to handle the gasoline oil supply.
Background technology
The method of removing for the gas-state hydrocarbon of existing employing adsorption-desorption agent, be following method of carrying out: the gas (waste exhaust gases that contains the gasoline vapor of about 40vol%) that will take place from waste exhaust gases generation source, is discharged into the waste exhaust gases of handling of the absorption process that is through with the atmosphere as the air (Purge gas) that contains 1vol% or following gasoline vapor from the top of adsorption tower (be converted to desorption step then be adsorption tower) by discharge pipe by the waste exhaust gases snorkel adsorption tower of supplying gas by air blast (blower) or self pressure.
Under such situation, adsorption tower switches mutually between above-mentioned absorption process and desorption step described later on one side, on one side running, its switching time, (Swing Time) was about 5 minutes.
On the other hand, in the adsorption tower behind the absorption process that is through with, send purge gas, attract to carry out desorb by vavuum pump by the purge gas snorkel.As purge gas, use the part of the Purge gas of when the absorption running, discharging from the adsorption tower top, vavuum pump turns round under about 25Torr.
The Purge gas that contains gasoline vapor after the desorb is supplied gas by snorkel in the gasoline recover, contacts with liquid gasoline by distributing pipe, as the gasoline vapor in liquid (gasoline absorption liquid) the reclaiming clean waste gas.
In waste exhaust gases from the gasoline recover, owing to there is a spot of gasoline vapor, so turn back to once more in the waste exhaust gases pipe by the foldback pipe, carry out adsorption treatment with the waste exhaust gases that the source takes place from waste exhaust gases, also have, recirculated cooling water is with the adsorbent layer in the cooling adsorption tower in inner core.
By such formation, can with gasoline vapor almost full dose reclaim as liquid gasoline, the concentration of the gasoline vapor of discharging from adsorption tower becomes very low, can reach the level (for example with reference to patent documentation 1) that does not cause atmosphere pollution.
No. 2766793 communique of [patent documentation 1] patent (the 3-6 page or leaf, Fig. 1)
Summary of the invention
In the recovery method of the employing vavuum pump desorb gasoline vapor of patent documentation 1, it is quite big that the power capacity of pump becomes, so impracticable.
In addition,, adsorption tower need be done greatly, perhaps shorten the switching time (Swing Time) of absorption and desorb, when using big adsorption tower, have the problem of area and the problem of adsorbent cost etc. of being provided with for a large amount of waste exhaust gases of full dose adsorption treatment.In addition, if shorten switching time, existence is the gasoline vapor that adsorbs of desorb fully, perhaps shortens the problem in the life-span of valve etc.
Further, necessarily contain airborne moisture in the gasoline vapor, in existing mode, because while absorbing gasoline steam and this moisture, so the problem that exists the absorption property of adsorbent to descend.
In addition, gasoline vapor only takes place in the occasion of the gasoline vapor that leaks when being used to reclaim oil supply when oil supply, and this frequency takes place according to sky or hour variation, is dissimilar.Under such occasion, conventional device is owing to switch absorption and desorb at certain intervals, so in the occasion of oil supply hardly such as usual night, gasoline vapor does not flow out fully, can produce the but problem of the such waste of desorb of amount that not absorption needs.
The present invention is the invention of carrying out in order to address the above problem, and its purpose is to provide and prevents to make processing, retracting device and method that adsorbent is poisoned, further small-sized and cheap gas-state hydrocarbon owing to be contained in moisture in the gasoline vapor.
The processing of gas-state hydrocarbon of the present invention, retracting device possess the condensing unit of removing moisture and gasoline vapor, at the adsorption-desorption device of the gasoline vapor of the gas downstream side design of the back segment of this condensing unit.
The processing of the gas-state hydrocarbon that the present invention relates to, recovery method are in having each adsorption-desorption device of one of adsorption tower and desorber at least, means with this adsorption-desorption device of cooling, as adsorbent, use the silica gel or the synthetic zeolite of aperture 4-100 dust, form with independent or mixture, carry out adsorption-desorption at low temperatures, further the part of the exit gas of adsorption tower is delivered in the desorber, the gas when using desorb is as Purge gas.
The present invention removes the condensing unit of moisture and gasoline vapor and the adsorption-desorption device of gasoline vapor by setting, can make waste exhaust gases fully purify (gasoline concentration is at 1Vol% or following), and can realize small-sized and cheap gasoline vapor retracting device.Especially,, do not worry that adsorbent is poisoned by moisture yet, in the pipe arrangement of condensing unit or adsorption-desorption device, do not freeze simultaneously yet, therefore can realize stable running action even in gasoline vapor, contain the occasion of moisture.
In addition, the temperature by the control thermal medium is in uniform temperature, and the temperature of control condensing unit and adsorption-desorption device is compared with occasion of each device of control respectively, can make the control circuit simplification, can realize low cost.In addition, no matter adsorption-desorption, the temperature of adsorption tower is all certain, so can reduce in order to cool off the adsorption tower energy needed, can realize saving the gas and oil vapour-recovery unit of energy.Have again,, can also can reduce the use amount of adsorbent with a large amount of gasoline vapor of quite few adsorbents adsorb in order to cool off adsorption tower.
Further, can obtain following remarkable result: the unusual temperature that can suppress in the adsorption tower that heat of adsorption brings rises, and makes the temperature homogenization in the adsorbent equipment, security that can very relieved adsorbent equipment.
The simple declaration of accompanying drawing
Fig. 1 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 1, and expression is provided with the example of 1 condensing unit.
Fig. 2 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 1, and expression is provided with the example of the 1st condensing unit and the 2nd condensing unit.
Fig. 3 is with the oblique view shown in in-built a part of otch of the adsorption-desorption tower of Fig. 1, Fig. 2.
Fig. 4 is the performance plot that is used to illustrate the control method of the purified gas scale of construction.
Fig. 5 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 2.
Fig. 6 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 3.
Fig. 7 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 4.
Fig. 8 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 5.
Fig. 9 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 6.
Figure 10 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 7.
Figure 11 is the pie graph of layout of processing, retracting device of the gas-state hydrocarbon of expression Figure 10.
Figure 12 is with the oblique view shown in in-built a part of otch of the adsorption-desorption tower of Figure 10.
Figure 13 is the performance plot that is used to illustrate the control method of the purified gas scale of construction.
Figure 14 is used to illustrate desorption time and adsorption-desorption tower internal pressure and the performance plot of the relation of the gasoline concentration of discharging from the adsorption-desorption tower.
Figure 15 is the performance plot of the relation of the gasoline concentration that is used to illustrate adsorption-desorption tower internal pressure and the gas flow of discharging from the adsorption-desorption tower, discharges from the adsorption-desorption tower and the gasoline vapor flow of discharging from the adsorption-desorption tower.
Figure 16 is used for illustrating that the gasoline of adsorption-desorption tower internal pressure and condensing unit reclaims the performance plot of the relation of flow.
Figure 17 carries out the oblique view shown in the otch with the in-built part of the adsorption-desorption tower of the processing of the gas-state hydrocarbon of embodiments of the present invention 8, retracting device.
Figure 18 is the processing of the gas-state hydrocarbon of expression embodiments of the present invention 9, the gas circulation air blast and the pump structure figure of retracting device.
Figure 19 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 10.
Figure 20 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 11.
Figure 21 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 12.
Figure 22 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 13.
Figure 23 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 14.
Figure 24 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 14.
Figure 25 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 15.
Figure 26 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 15.
Figure 27 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 16.
Figure 28 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 17.
Figure 29 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 17.
Figure 30 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 18.
Figure 31 is that the in-built part of desorber of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 19 is carried out the oblique view shown in the otch.
Figure 32 is the sectional drawing of the adsorption-desorption tower of Figure 31.
Figure 33 is all pie graphs of outward appearance of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 20.
Figure 34 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 21.
Figure 35 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 22.
The explanation of symbol
Source (giving oil nozzle) takes place in 1 waste exhaust gases, 2,3 adsorption-desorption towers, 4 gas circulation air blast (pump), 5 liquified petroleum recovers, 6 condensing units, 7 the 2nd condensing units, 8 pumps, 9 gas-liquid separators, 11 waste exhaust gases snorkels, 12a, the 12b discharge pipe, 13a, 13b Purge gas snorkel, 14a, Purge gas snorkel after the 14b desorb, 21 silica gel, 22 fin-tube heat exchangers, 41 pressure gauges, 120a, the 120b pressure controller, 201 refrigerators, 202 liquid circulation pumps, 203 heat exchangers, 204 medium temperature grooves, 205 auxiliary temperature media slot, 211 injectors, 212 gasoline concentration sensors, 213 thermometers, 214 pressure-regulating valves, 215 filters, 216 temperature sensors, 217 pressure sensors, 218 gas lines, 219 dry airs generate machine, 220 gas retention basins, 221 fire extinguishers, 301 ventilation voids, B13a, the B13b mass flow controller, B101a, the B101b constant flow rate valve, B103a, the B103b constant pressure valve, R1, R2, R3a, R4a, R3b, the cold medium of R4b gateway, R5, R6 hot gas gateway, H1, the H2 heater
The specific embodiment
[embodiment 1]
Fig. 1 and Fig. 2 are the processing of the gas-state hydrocarbon of expression embodiment of the present invention 1, whole pie graphs of retracting device flow process, and Fig. 1 has represented to design the example of 1 condensing unit, and Fig. 2 has represented to design the example of the 1st condensing unit and the 2nd condensing unit.Fig. 3 is the oblique view of expression with the internal structure part otch of the adsorption-desorption tower of Fig. 1, Fig. 2, and Fig. 4 is the performance plot that is used to illustrate the control method of Purge gas flow.
Among Fig. 1, Fig. 2, the oil nozzle of giving in source takes place in 1 expression as waste exhaust gases, the 8th, be used for from sucking the pump of gasoline vapor for oil nozzle 1, the 6th, condensing unit (being the 1st condensing unit among Fig. 2), 7 is the 2nd condensing units, the 9th, and gas-liquid separator, the 5th, liquified petroleum recover, 2, the 3rd, as the adsorption-desorption tower of adsorption-desorption device, the 4th, gas circulation air blast (pump).B1 is to the valve that is closing beyond the 1 oil supply time of oil nozzle, the 11st, gasoline vapor snorkel, B11a that condensing unit 6 or the 1st, the 2nd condensing unit 6,7 are connected with adsorption- desorption tower 2,3, B11b is the absorption valve of the adsorption- desorption tower 2,3 that is provided with in the way of gasoline vapor snorkel 11,12a, 12b are provided in a side of the discharge pipe to atmosphere at the top of adsorption- desorption tower 2,3, and 120a, 120b are arranged on the pressure controller on this discharge pipe 12a, the 12b.
In addition, 13a, 13b are the Purge gas snorkels, be used for and deliver to desorber 3 or 2 from the part that adsorption tower 2,3 is discharged to the clean air of atmosphere as Purge gas, B13a, B13b are arranged on the mass flow controller of the control gas flow on this Purge gas snorkel 13a, the 13b, 14a, 14b are the Purge gas ajutages that connects after the desorb of gas circulation blower 4 and adsorption- desorption tower 2,3, and the separating of adsorption- desorption tower 2,3 that B14a, B14b are arranged on this Purge gas ajutage 14a, the 14b smokes valve.R1, R2 are the entrance and exits of the cold medium of discrepancy condensing unit 6, R3, R4 are the entrance and exits of cold medium of more low temperature of the 2nd condensing unit 7 of coming in and going out, R3a, R4a, R3b, R4b are the entrance and exits of the cold medium of low temperature of adsorption- desorption tower 2,3 of coming in and going out respectively, and R41 is arranged on the pressure gauge of gas circulation with the exhaust side of air blast 4.
Next, the processing of the gas-state hydrocarbon of Fig. 1, the action of retracting device are described.When the gas station began oil supply, pump 8 actions sucked from the gasoline vapor (normal temperature is about 40Vol% down) of spilling for oil nozzle 1, for example are pressurized to about 0.3MPa, and the body of supplying gas is to condensing unit 6.The inside of condensing unit 6 makes it be passed to outlet R2 by cold medium is imported from inlet R1, remain on about 5 ℃, contained moisture part condensation in gasoline and the gas, be separated into gas (gasoline vapor) and liquid (gasoline) by gas-liquid separator 9, the downside of condensing unit 6 is stayed in the liquid storage, in liquified petroleum recover 5, gas is discharged from condensing unit 6 as liquids recovery.Import gasoline vapor by the top from condensing unit 6 and be passed to the below, the gasoline of liquefaction and moisture flow to the below efficiently by gravity and air-flow, make these liquefaction things of recovery become easy.
But the concentration of gasoline vapor reaches about about 10Vo l% under the operating condition 0.3MPa of condensing unit 6,5 ℃ condition.There are the situation import in adsorption- desorption tower 2,3 and the situation of as shown in Figure 2 further importing 2nd condensing unit 7 thereafter.This situation is as follows.
Next, the gasoline vapor about the 10Vol% that the 1st condensing unit 6 fails to handle is supplied gas and is handled in the 2nd condensing unit 7.In the 2nd condensing unit 7, the colder medium of low temperature is to outlet R4 circulation than the 1st condensing unit 6 by importing from inlet R3, and such the 2nd condensing unit 7 is set in more low temperature, for example-10 ℃ about.In the 2nd condensing unit 7, gasoline and moisture and the 6 same condensations of the 1st condensing unit are reclaimed.Situation in temperature running below freezing is also arranged in the 2nd condensing unit 7,, worry sometimes because the ice that produces in the 2nd condensing unit 7 stops up the situation of the gas passage in the 2nd condensing unit 7 according to the occasion difference.For fear of such problem, stop the circulation of cold medium at regular intervals, the cold medium of the high temperature that perhaps circulates etc., the operation that increases dissolving ice (thawing) in advance is effective.In addition, the device (not illustrating among the figure) that can measure the pressure loss is set in the 2nd condensing unit 7, if the pressure loss surpasses setting value, the program (sequence) that assembling adds the operation of thawing is also passable.Certainly, other means that use can detect the icing state of the 2nd condensing unit 7 detect the state of freezing, if produce ice, the program that assembling moves to the operation of thawing is also passable.
The concentration of gasoline vapor reaches about about 5Vol% under the operating condition 0.3MPa of the 2nd condensing unit 7 ,-10 ℃ condition.This gasoline vapor is vented to processing in the adsorption-desorption tower 2,3.2 situations of moving as desorber as adsorption tower, 3 in Fig. 1, Fig. 2, have been provided.Therefore, valve B11a is an open state, and valve B11b is a closed condition.In adsorption tower 2, use as desorber after the time adsorption treatment arbitrarily.This occasion is closed at valve B11a, use under the B11b opened state.Further,, be re-used as adsorption tower and use, use this action in time repeatedly in gasoline desorb finish time.The switching controls of valve B11a, B11b is passed through in the switching of absorption, desorb as previously mentioned.
Gasoline vapor is supplied gas by snorkel 11 in the adsorption tower 2.Enclose the adsorbent of absorbing gasoline steam in the adsorption-desorption tower 2,3.As the adsorbent of gasoline vapor, use silica gel.It is effective having the independent silica gel in 4-100 dust aperture or synthetic zeolite or their mixture especially.Feed in this adsorbent absorption by gasoline vapor and remove gasolene ingredient, becoming gasoline concentration is 1Vol% or following pure air, and 12a is released in the atmosphere by discharge pipe.Adsorption tower 2 utilizes the cold medium or the additive method of low temperature to be cooled off by utilizing the 2nd condensing unit 7, seeks to remove because heat that absorption produces and increase adsorption capacity.In addition, by reducing the temperature inside of adsorption tower 2, can increase adsorption capacity.
But, also lower if the internal temperature of adsorption tower 2 is reduced to than the design temperature of the 1st condensing unit 6 or the 2nd condensing unit 7, in order to make water condensation in adsorption tower 2,, preferably set in almost identical temperature with condensing unit 6 in the occasion of having only condensing unit 6.In addition, in the occasion that has the 2nd condensing unit 7, preferably set into the design temperature of the 2nd condensing unit 7.Further, on discharge pipe 12a, the 12b of atmosphere, setting pressure controller 120a, the 120b that pressure is controlled at setting, making the pressure in the adsorption tower 20 maintain setting.In the occasion of Fig. 2 owing to use the waste exhaust gases of the high pressure (about 0.3MPa) of the 2nd condensing unit 7 to adsorb, so can improve adsorption capacity significantly than absorption under the normal pressure.
The internal structure of adsorption- desorption tower 2,3 as shown in Figure 3, consideration is to the heat transfer of silica gel 21 or synthetic zeolite or their mixture, configuration fin-tube heat exchanger (cold medium being flowed into heat-transfer pipe) 22 with aluminium fin (ア Le ミ Off イ Application), between the aluminium fin, fill in silica gel 21 or synthetic zeolite or its mixture, make air-flow fully mobile at upper and lower settings cowling panel 23 simultaneously.At this moment, gasoline vapor only flows between the aluminium fin, in order high efficiency to adsorb, is effective at the partially filled fluorine class of the passage of fin-tube heat exchanger 22 packing material.In addition, for the space in the passage part does not flow into gasoline vapor, also can seal the space of passage part.In addition, the 24th, shell, 25a, 25b are to go up lower flange, 26a, 26b be silica gel 21 prevent to flow out net.
At the leading portion of adsorption- desorption tower 2,3 occasion of condensing unit 6 or the 1st, the 2nd condensing unit 6,7 is not set, is contained in water adsorption in the gasoline vapor on adsorbent, the absorption property of gasoline vapor descends, and needs the above adsorbent of necessary amount.In addition, be reduced in occasion below freezing, have the situation of moisture dewfall in burdens such as adsorbent surface gas obstructions takes place in the temperature of adsorption tower 2.In the present embodiment owing to be provided with condensing unit 6 or the 1st, the 2nd condensing unit 6,7 at the leading portion of adsorption- desorption tower 2,3, so gasoline vapor remove with moisture, so can prevent the bad influence that is subjected to moisture in the adsorption-desorption tower 2,3.In addition, can be reduced in the amount of gasoline that adsorption- desorption tower 2,3 is handled significantly, so can make the miniaturization of adsorption-desorption tower, the cheap manufacturing.
In the present embodiment, in the occasion that has designed the 1st, 2 condensing units 6,7, the amount of gasoline of handling at adsorption- desorption tower 2,3 can be reduced to 5Vol% from the gasoline of giving the high concentration (40Vol%) that oil nozzle 1 reclaims at the 1st, 2 condensing units 6,7, so can be reduced to 12.5% (=5%/40%) with respect to whole traffic attractions.That is, by the leading portion at adsorption- desorption tower 2,3 the 1st, the 2nd condensing unit 6,7 is set, the volume that can make adsorption- desorption tower 2,3 is about 1/10.In addition, as shown in Figure 1, in the occasion of having only condensing unit 6, can be reduced to 10Vol%, therefore the gasoline full dose of handling with adsorption- desorption tower 2,3 can be reduced to 25% (=10%/40%) with respect to whole traffic attractions.Can make the volume of absorption adsorption tower 2,3 in this occasion is about 1/4.
Next desorption process is described.The occasion of the gasoline that adsorbs in the desorb adsorbent uses air blast 4 through gas from the adsorbent desorb gasoline of the attraction of the purified gas snorkel 14a after the desorbs from desorber 3 by gas circulation.At this moment valve B14a is open in advance, and valve B14b closes in advance.When absorption, move under the high pressure conditions of adsorption tower at 0.3MPa, when desorb,,, make the gasoline desorb that is adsorbed on the adsorbent so utilize this pressure differential owing to reduce pressure below the atmospheric pressure with air blast 4 by gas circulation.The gasoline vapor of desorb, turns back in the adsorption- desorption tower 2,3 after gasolene ingredient is reclaimed in condensation once more once more at the return condensed device 6 of the occasion of Fig. 1.Carrying out repeatedly between this operation, the gasoline condensation of full dose is recovered in the condensing unit 6.In the occasion of Fig. 2, turn back in the 2nd condensing unit 7, after gasolene ingredient is reclaimed in condensation once more, return once more in the adsorption-desorption tower 2,3.Carrying out repeatedly between this operation, the gasoline condensation of full dose is recovered in the 2nd condensing unit 7.
Only utilizing owing to the desorption method of gas circulation with the pressure differential of the attraction generation of air blast 4, because its efficient is not very high, is effective so Purge gas is imported from the outside.In the present embodiment, will deliver in the desorber 3 and use by discharge pipe 12, Purge gas snorkel 13a as the part that is discharged to the clean gas the atmosphere from adsorption tower 2 of this Purge gas.B13a, B13b are the mass flow controller of the gas flow that passes through of control, and at this moment, mass flow controller B13b is an open state, are the states of gas of ormal weight of can circulating, and mass flow controller B13b closes, and gas does not flow.Having, also can be constant flow rate valve in the occasion of setting certain gas flow again.
In addition, carry out the result of desorption experiment, the Purge gas flow is the occasion of 15-25L/min as can be known, is set at 100-300Torr by the internal pressure with adsorption tower, efficiently the desorb gasoline vapor.
Like that, it is a certain amount of also can when the gasoline vapor desorb Purge gas flow to be controlled at shown in Fig. 4 (a), like that, if can follow the time to change the Purge gas flow, then more effective shown in Fig. 4 (b).That is it is effective, following desorption time to increase the Purge gas flow.Because petrol vapor quantity is many, so there is no need a large amount of Purge gas, still the amount of gasoline along with the time desorb reduced after desorb began at once, so attract gas flow also to reduce.Therefore, increase the Purge gas flow, prevent that it is effective attracting the reduction of gas flow.The interior unnecessary gas of the system of sending into causes the power homenergic loss of gas circulation with air blast 4, so the flow-control of preferred neat oxidizing gases is in the needs Min..In addition, in the present embodiment, owing to fully reduce amount of moisture in the gas, the moisture that is contained in the Purge gas has not almost had the harmful effect of the adsorbent in the desorber 3 in the condensing unit 6 or the 1st of adsorption- desorption tower 2,3 leading portions, the 2nd condensing unit 6,7.
In addition, in the present embodiment, design temperature when the temperature in the time of need not be with the gasoline vapor desorb changes to absorption, carry out desorb by the displacement that utilizes the pressure variation and the purified gas scale of construction, in order further to improve desorption efficiency, also can be when desorb temporarily stop the circulation of the cold medium that flows, make temperature in the desorber 3 near room temperature from inlet R3b to outlet R4b at desorber 3.The temperature of temperature when making desorb during than absorption is also high, can realize more high efficiency desorb.Desorb finishes, and is the initial stage of adsorption process in transfer, the temperature height of adsorption tower, and absorption property is low, because not residual fully gasoline in the adsorbent does not spill so worry gasoline.Along with the process of time, the adsorbance of gasoline increases, and the temperature of adsorption tower also reduces simultaneously, and the absorption property of adsorbent is enhanced, so when desorb is shifted to adsorption process, there is no need to carry out rapidly the cooling of tower.Certainly, by forcing heating desorption tower 3 when the desorb, also can further improve desorption performance.But, because temperature disturbance, the energy consumption that has increased refrigerator and heater, so on energy during than adsorption-desorption temperature be that certain mode is poor.
In gasoline service station, oil supply is irregularly carried out.Therefore, the occasion of Fig. 2, from reducing the viewpoint of electricity usage amount, only the binding hours when oil supply makes pump 8 actions, reclaims from the gasoline vapor of leaking for oil nozzle 1.Therefore, pump 8 and the 1st condensing unit 6 intermittent runnings.On the other hand, utilize gas circulation with the closed-loop path circuit of air blast 4, promptly, comprise that the system of the 2nd condensing unit 7, adsorption- desorption tower 2,3 has adopted the formation of continuous running.In this closed-loop path circuit, during recyclegas, there is the danger of sucking air for oil nozzle 1, so insert valve B4 in advance in the front of gas circulation blower 4 from gasoline, when pump 8 stops, shut off valve 4, during pump 8 actions, the way of relief valve 4 is effective.By adopting such formation, can easily the pressure in the adsorption tower 2 always be remained on necessarily, make the operating stably of system become easy.
But carry out the occasion of oil supply hardly at night on ordinary days etc., owing in above-mentioned closed circuit, do not supply with new gasoline, so do not set pressure controller 120a, 120b, the situation that exists gas pressure to reduce gradually.At this moment, because this pressure of adsorption tower 2 reduces, worry to be adsorbed on that the gasoline desorb is put in the atmosphere on the adsorbent.Perhaps a part of excessive pressure in the closed circuit rises to safe ABL, worries to have to follow the danger of igniting.Therefore,, set pressure gauge 41 in gas circulation with the exhaust side of air blast 4 in advance,, stop gas circulation automatically, use such Security Countermeasures with air blast 4 in the occasion of the pressure limit that surpasses regulation in the occasion of Fig. 2.
[embodiment 2]
Fig. 5 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 2.
Present embodiment is with the different of embodiment 1, uses pump 8 to be returned to from the gasoline vapor of desorber 3 desorbs the 1st condensing unit 6.In the present embodiment, do not need the used gas circulation of Fig. 1 air blast 4.But if intermitten pump 8 when oil supply only, according to the running-active status of pump 8, the pressure of adsorption- desorption tower 2,3 changes, and has the situation that is difficult to adsorb control.Under this situation, by giving insertion valve B8 between oil nozzle 1 and the pump 8, pump 8 often turns round, and only opens this valve B8 when oil supply, and system can steady running.
[embodiment 3]
Fig. 6 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 3.
In above-mentioned embodiment 1, when the gasoline vapor desorb, the part of exit gas of using adsorption tower 2 is as Purge gas, in the present embodiment, as Purge gas, can further improve desorption efficiency by the high extraneous gas of serviceability temperature.Externally gas introduction port-Purge gas snorkel 13a, the last configuration of 13b valve B15a, B15b by the switch of these valves B15a, B15b, can control the purified gas scale of construction.Certainly as previously mentioned, can when the gasoline vapor desorb, supply with a certain amount of Purge gas, also can be along with the time changes the supply gas amount.
In the occasion of using extraneous gas as Purge gas, moisture contained in the extraneous gas also might be absorbed by the adsorbent in the desorber 3, so way such as use or dehumidifying back use is also effective sometimes under the not high situation of humidity.
[embodiment 4]
Fig. 7 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 4.
Present embodiment is not use Purge gas to carry out the mode of desorb gasoline vapor, even do like this,, becomes simply as system though desorption efficiency has descended, and also be favourable sometimes.Especially, in the occasion of not using Purge gas, owing to make that the adsorption conditions temperature is lower, pressure is higher, desorption condition is high temperature, low pressure, and pressure differential, temperature difference in the time of need be with adsorption-desorption be set big.
[embodiment 5]
Fig. 8 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 5.
Present embodiment is to substitute cold medium in desorber 3,, to outlet R6 circulation hot gas the temperature in the adsorption tower 3 is brought up to more than the room temperature from inlet R5, improves the mode of desorption efficiency.
[embodiment 6]
Fig. 9 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 6.
Present embodiment is by set heater H 1a, H1b on Purge gas snorkel 13a, 13b, by the Purge gas of heating, improves the mode of desorption performance.
[embodiment 7]
Figure 10 is whole pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiment of the present invention 7.
Present embodiment and embodiment 1 difference are, use refrigerator 201 chilling temperature media (salt solution liquid etc.), by liquid circulation pump 202 this medium temperature are supplied with condensing unit 6 and adsorption-desorption tower 2,3.Promptly, by making cold medium flow through heat exchanger 203 from refrigerator 201, make the medium temperature cooling of accumulating in the medium temperature groove 204 that is provided with heat exchanger 203, the medium temperature of cooling is supplied with condensing unit 6 and adsorption- desorption tower 2,3 by liquid circulation pump 202.In addition, the control of the temperature of medium temperature is by measuring the temperature of the medium temperature in the medium temperature groove 204, and the running of control refrigerator 201 is implemented.In addition, in Figure 10, show configuration condensing unit 6 in medium temperature groove 204, supply with the example of adsorption- desorption tower 2,3 by liquid circulation pump 202.
Among the figure, the 1st, give oil nozzle, the 8th as what the source took place waste exhaust gases, be used for from the pump, the 6th of sucking gasoline vapor for oil nozzle 1, condensing unit, the 9th, gas-liquid separator, the 5th, liquified petroleum recover, 2, the 3rd, adsorption-desorption tower, the 4th, gas circulation is at the valve, the 11st of closing for oil nozzle 1 oil supply outside the time with air blast, B1, connects gasoline vapor snorkel, the B11a of condensing unit 6 and adsorption-desorption tower 2,3, B11b is the absorption valve of the adsorption-desorption tower 2,3 that is provided with in the way of gasoline vapor snorkel 11.The 120th, the pressure controller of adjusting adsorption-desorption tower 2,3 pressure, 12a, 12b are the discharge pipes that connects adsorption-desorption tower and pressure controller 120, B12a, B12b is exhaust valve, the 13a at the adsorption-desorption tower 2,3 that is provided with of this discharge pipe 12a, 12b midway, 13b is used for a part that is discharged to the clean air of atmosphere from adsorption tower 2 or 3 is delivered to desorber 3 or 2 and the Purge gas snorkel, the B13a that use as Purge gas, and B13b is arranged on the mass flow controller of the control gas flow on this purge gas snorkel 13a, the 13b.
14a, 14b connects gas circulation blower 4 and adsorption-desorption tower 2, Purge gas ajutage after 3 the desorb, B14a, B14b is arranged on this Purge gas ajutage 14a, adsorption-desorption tower 2 on the 14b, 3 separate smokes valve, the 201st, cooling condensation device 6 and adsorption- desorption tower 2,3 refrigerator, the 202nd, will supply with adsorption-desorption tower 2 by the medium temperature of refrigerator 201 coolings, 3 liquid circulation pump, the 203rd, the heat of the cold medium supplied with from refrigerator 201 is passed to the heat exchanger of medium temperature, the 204th, fill medium temperature groove by the medium temperature of heat exchanger 203 coolings.
At first, the formation to device describes.Figure 11 is the processing of the gas-state hydrocarbon of expression embodiment of the present invention, the figure of retracting device layout.As shown in figure 11, on the top of ventilation voids (air gap) 301 refrigerator 201 only is set.That is, directly contact with gasoline vapor, be arranged on the top of ventilation voids 301 in order not make refrigerator 201.Thus, refrigerator 201 is arranged on outside the scope in flammable steam delay place, and flammable steam can be owing to refrigerator 201 catch fire, so become safe setting.On the other hand, other machine, promptly, pump 8, condensing unit 6, gas-liquid separator 9, adsorption- desorption tower 2,3, gas circulation blower 4, valve B11a, B11b, B12a, B12b, B14a, B14b, mass flow controller B13a, B13b, and pressure controller 120 (not illustrating among these a part of figure) is arranged on flammable steam and is detained the place owing to contact with gasoline vapor.In addition, for being arranged on the e-machine that flammable steam is detained the place,, make blast resistance construction in order to ensure security.
In addition, liquid circulation pump 202 and medium temperature groove 204 should be arranged on the top of ventilation voids 301 usually owing to do not contact with gasoline vapor.But liquid circulation pump 202 is arranged on the top of ventilation voids 301, liquid circulation pump 202 is in the position also higher than the adsorption- desorption tower 2,3 of supplying temperature medium, make the air interlock takes place in the liquid circulation pump 202, worry to produce the problem that to cool off adsorption-desorption tower 2,3.Therefore, making the liquid circulation pump 202 of blast resistance construction and medium temperature groove 204 is placed on flammable steam to be detained the place is effective.In addition, need know the content of medium temperature contained in the medium temperature groove 204 in advance.That is, as representing (not illustrating among the figure) such as pipes by liquid level meter or water level are set, the content of monitor temperature medium is known the reduction etc. of the cooling capacity of device, so safer retracting device can be provided.
Next, action is described.When the gas station began oil supply, pump 8 actions sucked from the gasoline vapor (normal temperature is about 40Vol% down) of spilling for oil nozzle 1, for example are pressurized to about 0.3MPa, and the body of supplying gas is to condensing unit 6.If the condensing unit 6 that has in the medium temperature groove 204, is cooled by medium temperature the heat exchanger 203 in the cold medium supplying temperature media slot 204 indirectly from refrigerator 201.Usually, the inside of condensing unit 6 remains on about 0 ℃-5 ℃, contained moisture part condensation in gasoline and the gas, be separated into gas (gasoline vapor) and liquid (gasoline) by gas-liquid separator 9, the downside of condensing unit 6 is stayed in the liquid storage, in liquified petroleum recover 5, gas is discharged from condensing unit 6 as liquids recovery.Import gasoline vapor by the top from condensing unit 6 and be passed to the below, the gasoline of liquefaction and moisture flow to the below efficiently by gravity and air-flow, make these liquefaction things of recovery become easy.
But, be that the concentration of gasoline vapor becomes about 10Vol% under the condition of pressure 0.3MPa, 5 ℃ of chilling temperatures, gas flow 60L/min at the operating condition of condensing unit 6.In addition, as from the saturated concentration curve map of gasoline vapor as can be known, the saturated vapor oil vapor concentration under 5 ℃ of pressure 0.3MPa, temperature is about 10vol%, and gasoline vapor concentration is not at 10vol% or following in theory under this condition.By reducing temperature, can be reduced in the gasoline vapor concentration of the outlet of condensing unit 6.But, if the water that design temperature below freezing, is contained in the gas freezes in condensing unit 6, the pipe arrangement blocking problem can take place, so the design temperature of condensing unit 6 is preferably about 0 ℃-5 ℃.
Next, the gasoline vapor about the 10Vol% that will fail to handle in condensing unit 6 is supplied gas and is handled in the adsorption-desorption tower 2,3.Figure 10 illustrates 2 situations when moving as desorber as adsorption tower, 3.Therefore, valve B11a open (painting black), B11b (do not have blacking, blank) be closed condition.Adsorption tower 2 uses as desorber after the adsorption treatment at any time.In this occasion, valve B11a close, B11b uses under opened state.Further,, be re-used as adsorption tower and use, use this action in time repeatedly in the moment that the desorb of gasoline finishes.Like that by transfer valve B11a, B11b controls as described above in the switching of absorption, desorb.
Gasoline vapor is supplied gas by snorkel 11 in the adsorption tower 2.Enclose the adsorbent of absorbing gasoline steam in the adsorption-desorption tower 2,3.As the adsorbent of gasoline vapor, use silica gel.Especially, it is effective having the independent silica gel in 4-100 dust aperture or synthetic zeolite or their mixture.Remove gasolene ingredient by gasoline vapor by absorption in this adsorbent, become gasoline concentration 1Vol% or following pure air, 12a is released in the atmosphere by discharge pipe.At the discharge pipe 12a to atmosphere, the downstream of 12b sets the pressure controller 120 of controlled pressure at setting, so that the pressure in the adsorption tower 2 is maintained setting.In the present embodiment,, can improve adsorption capacity significantly than absorption under normal pressure owing to use the waste exhaust gases absorption of the high pressure (about 0.3MPa) of condensing unit 6.
It doesn't matter in the effect of the adsorption-desorption of adsorption- desorption tower 2,3 and gasoline vapor, usually is cooled to uniform temperature by the medium temperature of being supplied with by liquid circulation pump 202.That is, usually the cooling system of running control condensing unit 6 and adsorption- desorption tower 2,3 makes it maintain design temperature.This is that be absolutely necessary cool time to a certain degree, can not deal with the cause of momentary operation owing to be cooled by the silica gel 21 of filling in the heat transfer adsorption- desorption tower 2,3 of fin-tube heat exchanger 22.Further be because, can not provide cheap gasoline recovery plant for the cost that can possess 201 pairs of equipment of the big refrigerator of cooling capacity in the short time cooling brings bad influence.Have again,, can increase adsorption capacity, reduce the use amount of silica gel 21 by reducing the internal temperature of adsorption tower 2.If but the internal temperature of adsorption tower 2 is also lower than the design temperature of condensing unit 6, water condensation in adsorption tower 2 is further frozen in occasion below freezing, so preferably set in the temperature almost same with condensing unit 6.
From the above fact, maintain the temperature of setting for the cooling system that makes condensing unit 6 and adsorption- desorption tower 2,3, and for the pressure system that makes condensing unit 6 and adsorption- desorption tower 2,3 maintains setting pressure, often can be by running control, carrying out efficiently, gasoline reclaims.
The external structure of adsorption-desorption tower 2,3 is made cylindrical conformation shown in Figure 12 (a).By making such structure, can make the pressure homogenization that drops on the wall, even the pressure in the adsorption-desorption tower 2,3 reach about 0.3MPa, also can be to realize safely, the adsorption-desorption tower 2,3 of warpage etc. does not promptly take place.In addition, the internal structure of adsorption-desorption tower 2,3 is considered to silica gel 21 or synthetic zeolite and is conducted heat, configuration fin-tube heat exchanger (medium temperature being flowed in heat-transfer pipe) 22 by the aluminium fin, between the aluminium fin, fill in silica gel 21 or synthetic zeolite, simultaneously flow out and prevent net 24 designing silica gel up and down, prevent that silica gel from flowing out pipe arrangement, makes gas flow good simultaneously.In this occasion, be adsorbed on the silica gel 21 in order to make the gasoline vapor homogeneous, gasoline vapor homogeneous in adsorption-desorption tower 2,3 is flowed, the cowling panel 23 with making such as punch metals also can be set.The fin of fin-tube heat exchanger 22 towards the pressure in order not damage gasoline vapor and to flow, the mobile direction of itself and gasoline vapor is provided with abreast.That is, in the situation of Figure 12 (a), flow from bottom to top in order to make gasoline vapor, at the stacked fin of transverse direction.In addition, for efficient cooling is filled near the outer wall silica gel 21, very close to each other between fin-tube heat exchanger 22 and outer wall is necessary.
This occasion, shown in Figure 12 (b), for having passage one side, be provided with and partly contact such clathrate or tabular metal (aluminium or the copper of heat-transfer character excellence are the most suitable) with passage, there be not passage one side, the length of the fin by making fin-tube heat exchanger 22 itself is elongated, and it is effective making very close to each other between outer wall and the fin-tube heat exchanger 22.In addition, in order to make 22 parts very close to each other of outer wall and fin-tube heat exchanger, also can insert metal bar or finned pipe etc.In addition, the occasion of circulation medium temperature in the heat-transfer pipe of fin-tube heat exchanger 22, the pipe arrangement branch that medium temperature is flowed is divided into multistage with fin-tube heat exchanger 22, and medium temperature is flowed side by side.Thus, the pressure loss of the mobile pipe arrangement of medium temperature can be reduced, the capacity of medium temperature being supplied with the liquid circulation pump 202 of adsorption- desorption tower 2,3 can be reduced.
Further, in this case, because gasoline vapor flows from bottom to top, net 24 from joining disposes like that so the silica gel of fin-tube heat exchanger 22 and bottom is flowed out prevent.Thus, flow out at silica gel and to prevent between net 24 and the fin-tube heat exchanger 22, can not spacing, that is, do not stay the space that only is filled with silica gel 21, the cooling of silica gel 21 in the time of can fully implementing to adsorb.Its result can prevent that the temperature of the silica gel 21 that part that the gasoline vapor in the highest gasoline concentration enters exists from rising, and safe adsorption- desorption tower 2,3 can be provided.In addition, in the occasion of the gasoline vapor that circulates from top to bottom, much less the silica gel on top flows out and prevents that net 24 and fin-tube heat exchanger 22 from joining.
The occasion of condensing unit 6 is not set at the leading portion of adsorption- desorption tower 2,3, the gasoline vapor of adsorption- desorption tower 2,3 middle and high concentrations flows into, be contained in water adsorption in the gasoline vapor simultaneously on adsorbent, the absorption property of gasoline vapor descends, and needs the above adsorbent of necessary amount.In addition, be reduced to occasion below freezing, have the situation of moisture in burdens such as adsorbent surface dewfall gas obstructions takes place in the temperature of adsorption tower 2.
In the present embodiment owing to be provided with condensing unit 6 at the leading portion of adsorption- desorption tower 2,3, so moisture remove with gasoline vapor, so can prevent the bad influence that is subjected to moisture in the adsorption-desorption tower 2,3.In addition, can be reduced in the amount of gasoline that adsorption- desorption tower 2,3 is handled significantly, so can make the miniaturization of adsorption-desorption tower, the cheap manufacturing.Further, in the present embodiment, the amount of gasoline of handling at adsorption- desorption tower 2,3 condensing unit 6, can be reduced to 10Vol% from the gasoline of giving the high concentration (40Vol%) that oil nozzle 1 reclaims, so can be reduced to 25% (=10%/40%) with respect to whole traffic attractions.That is, the leading portion design condensing unit 6 by at adsorption- desorption tower 2,3 can make the volume of adsorption- desorption tower 2,3 be about 1/4.
Next the desorption process to gasoline vapor describes.The occasion of the gasoline that adsorbs in the desorb adsorbent uses air blast 4 through gas from the strippant desorb gasoline of purified gas snorkel 14a attraction from desorber 3 by gas circulation.At this moment valve B14a is open in advance, and valve B14b closes in advance.Under the high pressure conditions of when absorption adsorption tower, move, when desorb, owing to reduce pressure below the atmospheric pressure with air blast 4,, be adsorbed on gasoline on the adsorbent by desorb so utilize this pressure differential by gas circulation at 0.3MPa.Gasoline vapor after the desorb, turns back in the adsorption tower 2 after gasolene ingredient is reclaimed in condensation once more once more at the return condensed device 6 of the occasion of Figure 10.Carrying out repeatedly between this operation, the gasoline condensation of full dose is recovered in the condensing unit 6.In addition, during desorb, by rising desorber 3 temperature inside, though can improve desorption rate, but, there is the problem that to carry out the switching of adsorption- desorption tower 2,3 at short notice simultaneously because temperature oscillation produces the energy that consumes in refrigerator and the heater and increases, so the temperature in when absorption is improved, to carry out desorb be effective to identical temperature during with absorption.
Gasoline vapor is arranged on the same part of adsorption- desorption tower 2,3 to the supply port of adsorption tower 2 when the outlet of the gasoline vapor of the desorber 3 during in addition, from desorb and absorption.Owing to be to make the gasoline vapor concentration of adsorption tower 2 outlets become 1vol% or the following adsorption tower 2 that uses like that, so become when absorption adsorption tower 2 the gasoline vapor suction inlet near absorbing gasoline steam to high-density, gasoline vapor almost not have the state that adsorbs near the gasoline vapor outlet of adsorption tower 2.The gasoline vapor of discharging from desorber 3 during for high efficiente callback desorb in condensing unit 6 need improve gasoline vapor concentration as best one can.Therefore in order to make the part of adsorbing from high density discharge the gasoline vapor that one of gasoline vapor can be discharged high concentration, preferably from the part of high density absorbing gasoline steam, that is, and near the gasoline vapor of when desorb, discharging of the gasoline vapor suction inlet of adsorption tower 2.
Only utilizing because in the desorption method of gas circulation with the pressure differential of the attraction generation of air blast 4, its efficient is not too high, is effective so import Purge gas from the outside.In the present embodiment,, will send pipe 13a by discharge pipe 12a, Purge gas from the part that adsorption tower 2 is discharged to the pure air of atmosphere and deliver to desorber 3 and use as this Purge gas.B13a, B13b are the mass flow controller of control by gas flow, and in this occasion, mass flow controller B13a is an open state, are the states of gas of ormal weight of can circulating, and mass flow controller B13b closes, and gas does not circulate.In addition, in the present embodiment, fully reduce the amount of moisture in the gas in the leading portion condensing unit 6, so the moisture that is contained in the Purge gas produces harmful effect to the adsorbent in the desorber 3 hardly.
Shown in Figure 13 (a), the Purge gas flow is a certain amount of in the time of also can controlling desorb.But, for recovery that the return condensed device 6 of the gasoline vapor of desorb is liquefied, discharge the gasoline vapor of high concentration as much as possible from desorber 3, this is the known fact.Further, send into unwanted gas and can cause gas circulation with the loss of the power homenergic of air blast 4 in system, to need Min. be effective so the purified gas scale of construction is controlled at.Therefore, shown in Figure 13 (b), like that, begin the back, be effective through the Purge gas of back importing after a while in desorb.That is, desorb has just begun the back because gasoline vapor is also many, thus do not need Purge gas, along with the amount of gasoline of effluxion owing to desorb reduces, so attract gas flow also to descend.Therefore, begin effectively to prevent to attract the reduction of gas flow from desorb to importing Purge gas through behind the certain hour.
Importing timing as Purge gas, can consider to use timer etc. to begin through importing the mode (timing mode) of Purge gas behind the certain hour from desorb, import the mode (pressure instrumentation mode) of Purge gas when the internal pressure of desorber 3 reaches setting value, the gas flow of the gasoline vapor of discharging from desorber 3 imports the mode (gas flow instrumentation mode) of Purge gas when reaching setting value.Though timing mode is the most favourable on the initial cost this point, the timing mode that imports Purge gas according to the amount of gasoline of adsorption-desorption tower 2,3 absorption may worry to reduce the validity that Purge gas imports.That is,, when in desorber 3, enough gasoline vapors being arranged, import Purge gas, reduced the gasoline vapor concentration of discharging thus from desorber 3 if adsorbance is many.On the contrary, if adsorbance is few, the time band that the gasoline vapor gas flow of discharging from desorber is few increases, and can not effectively eject the gasoline vapor from desorber 3.Pressure instrumentation mode and gas flow instrumentation mode can solve the problem of aforesaid timing mode, can realize desorb efficiently.In addition, in this gasoline recovery plant, on the safety on the piping system that gasoline vapor flows the setting pressure meter be integral.Therefore and since pressure instrumentation mode can with these pressure gauge dual-purposes, so think in 3 kinds of modes the most effective.
Figure 14 represents to change from the pressure of adsorption- desorption tower 2,3 with gasoline vapor change in concentration and adsorption-desorption tower at that time 2,3 outlet of the adsorption- desorption 2,3 of the occasion of 20NL/min discharge gasoline vapor.Adsorption conditions is that gasoline concentration is 10vol%, and pressure is 300kPa, so these values become initial value when desorb begins.In addition, the importing of Purge gas becomes negative pressure at the pressure of adsorption- desorption tower 2,3, that is, begin when arriving 100kPa.So as can be known, the internal pressure of adsorption- desorption tower 2,3 becomes negative pressure, and gasoline vapor concentration is maximum when arriving flex point (arrival stability region), and gasoline concentration slowly reduces thereafter.Therefore, as can be known in order in condensing unit 6, to reclaim the gasoline vapor of desorb, the exit concentration that the concentration of the gasoline vapor of desorb need be made as condensing unit 6 be 10vol% or more than, by keeping gasoline concentration as far as possible longways is 10vol% or above time band, can reclaim gasoline efficiently.
The figure of the relation of the gasoline vapor flow that gasoline vapor concentration that Figure 15 is the internal pressure of the adsorption-desorption tower 2,3 when investigating the gasoline vapor desorb and Purge gas flow, discharge from adsorption-desorption tower 2,3 and time per unit are discharged from the adsorption-desorption tower.So as can be known, in order to reduce the internal pressure of adsorption-desorption tower 2,3, can reduce the flow of Purge gas.In addition, as can be known by reducing the internal pressure of adsorption-desorption tower 2,3, can improve from the concentration of the gasoline vapor of adsorption-desorption tower 2,3 discharges.Therefore, the time per unit of the product representation of the gas flow (Purge gas flow) of discharging from adsorption-desorption tower 2,3 and the gasoline vapor concentration of discharging from adsorption-desorption tower 2, the 3 gasoline vapor flow of discharging from adsorption-desorption tower 2,3 is when the internal pressure of adsorption-desorption tower 2,3 is high as can be seen, so diminish because gasoline vapor concentration is low, have again, thus when the internal pressure of adsorption-desorption tower 2,3 is low because little the diminishing of air-flow of discharging.That is, there are the suitableeest zone jointly in internal pressure, discharge gas flow (the purified gas scale of construction) in running as can be known.But in this retracting device, discharging gasoline vapor from adsorption-desorption tower 2,3 is not main purpose, and the gasoline vapor that reclaims how many discharges is only main purpose.Therefore, as previously mentioned, in order to reclaim at condensing unit 6, need make in the gas of discharge gasoline concentration 10vol% or more than, how much desorb concentration is important if improving from 10vol%.
Figure 16 is the figure of relation of the yield hourly of the internal pressure of the adsorption- desorption tower 2,3 when investigating the gasoline vapor desorb and the gasoline vapor of discharging from adsorption-desorption tower 2,3.In addition, the gasoline yield of time per unit can with the concentration of the gasoline vapor of discharging and difference that the recovery critical concentration the condensing unit 6 is 10vol% from adsorption- desorption tower 2,3, with the product representation of the gas flow (Purge gas flow) of discharging from adsorption-desorption tower 2,3.The gasoline yield of time per unit is the highest when so as can be known, internal pressure being set at the 30kPa left and right sides.As described above owing to be about 75% in the rate of recovery of condensing unit 6, so need make desorb gasoline vapor the rate of recovery also 75% or more than.This is because if the organic efficiency of the gasoline vapor of desorb reduces, and does not reclaim in condensing unit 6, just increases the gasoline vapor that moves to adsorption tower 2 from desorber 3, the cause that reduces as the running efficiency of retracting device.
Therefore, must the petrol vapor quantity of supplying with adsorption tower 2 be recovered in 75% or above condition under, desorb is from the gasoline vapor of desorber 3.Promptly, because supplying with the gas flow of adsorption tower 2 is 60N/min, gasoline vapor concentration is 10vol%, and the petrol vapor quantity that time per unit is supplied with adsorption tower 2 is 6NL/min, thus need make time per unit from the gasoline yield of desorber 3 be 4.5NL/min or more than.Hence one can see that, need make internal pressure in the adsorption- desorption tower 2,3 at 15-40kPa.In addition, as shown in Figure 15,, need make the Purge gas flow at 15-35NL/min in order to make pressure in the adsorption- desorption tower 2,3 at 15-40kPa.
Above result by making discharge gas flow (Purge gas flow) from desorber 3 at 15-35NL/min, makes pressure in the adsorption tower 2 at 15-40kPa, expeditiously the desorb gasoline vapor as can be known.
In gasoline service station, oil supply is irregularly carried out.Therefore, from cutting down the viewpoint of electricity usage amount, only the finite time when oil supply makes pump 8 actions, reclaims from the gasoline vapor of leaking out for oil nozzle 1.Therefore, only in this occasion, become the pure air in 1vol% or following gasoline concentration from adsorption tower 2,12a is released in the atmosphere by discharge pipe.In this retracting device, in order to be used for from the air that adsorption tower 2 is discharged discharging gasoline from desorber 3, moving and move from the desorb of desorber 3 to the absorption of adsorption tower 2 usually is to carry out the same period.That is, usually turn round pump 8 and gas circulation under the state off and on air blast 4 in the same period.By such running, the gasoline vapor of desorb with the air dilution that air blast 4 is inhaled into, can not occur the reduction of the organic efficiency of condensing unit 6 by gas circulation.In addition, the gasoline vapor of desorb can not discharged from giving oil nozzle 1.Further, can prevent that also the air that contains abundant moisture in the desorber 3 is inhaled into.
Thus, by usually the same period turn round off and under state pump 8 and gas circulation can carry out gasoline expeditiously with air blast 4 and reclaim.In addition, the operating condition by proportioning pump 8 makes threshold switch, and it is certain often keeping the pressure in the adsorption- desorption tower 2,3 easily.
Next, the switching to adsorption- desorption tower 2,3 describes.In present embodiment, the occasion of using timer to carry out the switching of adsorption- desorption tower 2,3 describes.As previously mentioned, gasoline vapor is by adsorption tower 2, and gasolene ingredient is removed in absorption, becomes gasoline concentration at 1vol% or following pure air, and 12a is released in the atmosphere by discharge pipe.But along with the petrol vapor quantity of supplying with in the adsorption tower 2 increases, the adsorption capacity of adsorption tower 2 slowly reduces.If continue this state, during near 1vol%, just need to switch adsorption- desorption tower 2,3 in the gasoline concentration in the exit of adsorption tower 2.In gasoline service station, because oil supply is irregularly carried out, so, worry because the oil supply time in the occasion of switching by the time merely, can not know to have only which adsorption- desorption tower 2,3 to carry out the state of affairs of adsorption operations, discharge 1vol% or above gasoline vapor from retracting device.
Therefore, the switching of adsorption- desorption tower 2,3 is effective by the aggregate-value of gasoline recovery plant actuation time.That is, can reach the moment of stipulated time, carry out the switching of adsorption- desorption tower 2,3, reset its aggregate-value simultaneously, once more from carrying out the tired calculation of the duration of runs at first at the aggregate-value of gasoline recovery plant duration of runs.In addition, as the index of expression retracting device running, can enumerate the running of gas circulation with air blast 4 or pump 8.In this device, because gas circulation is with air blast 4 and running 8 same periods of pump, so tired to calculate which all no problem the duration of runs.In addition,,, do not switch at once, after the running of wait pump 8 stops, switching adsorption- desorption tower 2,3 and be fine even tired evaluation time reaches setting as the time that reality is switched.Thus, when supplying with adsorption- desorption tower 2,3 gasoline vapors, do not switch adsorption- desorption tower 2,3, on pump 8, do not apply excessive pressure, safe gasoline recovery plant can be provided.
At last, the processing of gas-state hydrocarbon, the control method of retracting device are described.When retracting device stops, stopping gas circulation air blast 4 and pump 8, valve B11a, B11b, B12a, B12b, B14a, B14b are full closing state, mass flow controller B13a, B13b are closed condition.When oil supply begins, accept commencing signal, for example, accept oil supply commencing signal corresponding to the switch motion of giving oil nozzle 1 as the oil supply signal from oil feeder, valve B11a, B12a, B14a is for opening state, the gas circulation that turns round thereafter air blast 4 and pump 8.If with the running of air blast 4, the pressure in the desorber 3 drop to normal concentration by gas circulation, the beginning of mass flow controller B13a opened, and the aperture of control mass flow controller B13a makes the flow of the regulation that flows in the desorber 3.After oil supply finishes, accept the stop signal from oil feeder, gas circulation stops with air blast 4 and pump 8, and mass flow controller B13a becomes closed condition, valve B11a, and B12a, B14a becomes closed condition.
Like this, oil supply if the aggregate-value of oil supply time reaches the stipulated time, is just carried out the switching of adsorption-desorption tower 2,3 repeatedly.But,, till accepting, also under the former state state, turn round from the stop signal of oil feeder even the oil supply aggregate-value reaches the stipulated time in the oil supply.If the stop signal of acceptance, then as previously mentioned, gas circulation stops with air blast 4 and pump 8, and mass flow controller B13a becomes closed condition, valve B11a, and B12a, B14a becomes closed condition.Then,, reset the cumulative time regularly if when accepting commencing signal from oil feeder, valve B11b, B12b, B14b becomes open state, and gas circulation is with air blast 4 and pump 8 runnings thereafter, and adsorption tower 3 becomes the absorption action, and desorber 2 becomes the desorb action.If by the running of gas circulation with air blast 4, when the pressure in the desorber 2 was reduced to normal concentration, mass flow controller B13b began to open, control the aperture of mass flow controller B13b, make the flow of the regulation that flows in the desorber 2.After oil supply finishes, accept the stop signal from oil feeder, gas circulation stops with air blast 4 and pump 8, and mass flow controller B13b becomes closed condition, valve B11b, and B12b, B14b becomes closed condition.Thereafter, till the oil supply cumulative time reaches the stipulated time, repeatedly should running.
In the above-described embodiment, to as the oil supply signal according to the switch motion of giving oil nozzle 1, receive oil supply and begin to be illustrated, but also can receive oil supply and begin and stop signal according to take action to oil nozzle 1 from oil feeder with the situation of stop signal.But, even this occasion under the state of breaking away from oil supply not for from oil feeder oil nozzle 1, the processing of this gas-state hydrocarbon, retracting device also can turn round, the retracting device that turns round under the state that does not suck gasoline vapor is from saving the viewpoint of energy existing problems.Therefore, such state continuance certain hour needs to carry in advance to stop the such controlling organization of retracting device.
As described above, the processing of the gas-state hydrocarbon of present embodiment, retracting device be because combination condensing unit 6 and adsorption- desorption tower 2,3, so even be only discharge maximum also only for the gasoline vapor of 1vol%, be processing, the retracting device of the very little gas-state hydrocarbon of carrying capacity of environment.In addition, even, can reclaim in the gasoline vapor of 40vol% to reach 39vol%, be that organic efficiency reaches 97.5% very high efficiency retracting device owing to a discharge maximum is the gasoline vapor of 1vol% only also.In addition, owing to after carrying out condensation operation, carry out adsorption operations, also has the effect that makes 2,3 miniaturizations of adsorption-desorption tower, all densifications of device.Further,, running useless can be reduced, operating cost can be reduced because the recovery of gasoline vapor is to carry out with the oil feeder interlock.
[embodiment 8]
Figure 17 is the figure that the device of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 8 constitutes.
Different with aforementioned embodiments 7 is that auxiliary temperature media slot 205 is arranged on the top of ventilation voids 301, simultaneously, places liquid circulation pump 202 above ventilation voids 301.According to present embodiment, do not need liquid circulation pump used in Figure 11 202 is made explosion-proof structure.But in liquid circulation pump 202, invade the occasion of gas (air etc.), produce the problem that to carry liquid sometimes.In order not cause such problem, by design auxiliary temperature media slot 205 above ventilation voids 301, gas is invaded in the liquid circulation pump 202, can the runs steadily system.
As described above, in the present embodiment,, can make the expense cheapness of liquid circulation pump 202, the processing of gas-state hydrocarbon, the cost of retracting device are reduced owing to do not need liquid circulation pump 202 is made explosion-proof structure.
[embodiment 9]
Figure 18 be expression embodiments of the present invention 9 gas-state hydrocarbon processing, retracting device gas circulation with compressor and pump structure figure.
In the processing of the gas-state hydrocarbon of present embodiment, retracting device, because the gas circulation that turns round simultaneously is with air blast 4 and pump 8, share motor 10 drives by belt pulley and to make gas circulation blower 4 and pump 8 runnings.Thus, the initial cost of motor 10 can be reduced, processing, the retracting device of cheap gas-state hydrocarbon can be supplied with.
[embodiment 10]
Figure 19 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 10.
In embodiment 7, show by flowing through adsorption- desorption tower 2,3, gasolene ingredient is adsorbed to be removed, become the clean air of 1vol% or following gasoline concentration, by discharge pipe 12a, be released to the situation in the atmosphere, and on discharge pipe 12a, be provided with injector (ejector) 211 in the present embodiment, further reduced the gasoline concentration of the gasoline vapor of discharging.Processing, the retracting device of safer gas-state hydrocarbon can be provided thus.
[embodiment 11]
Figure 20 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 11.
In embodiment 7, show the aggregate-value of the duration of runs of having calculated gas circulation usefulness air blast 4 or pump 8 in advance, its value has reached setting value, the occasion that stops at pump 8 is carried out the occasion of the switching of adsorption- desorption tower 2,3 then, and on discharge pipe 12a, be provided with gasoline concentration sensor 212 in the present embodiment, output valve from its gasoline concentration sensor 212 reaches setting value, and the occasion that stops at pump 8 is switched adsorption- desorption tower 2,3 then.Processing, the retracting device of safer gas-state hydrocarbon can be provided thus.In addition,, can enumerate gasolene ingredient is adsorbed on the semiconductor element, measure the semiconductor-type of the impedance of semiconductor element as gasoline concentration sensor 212; With use non-dispersion infrared line absorption method and measure the infrared ray absorbing formula of the ultrared uptake of about 3.3 mum wavelengths.
Like this, be 1vol% or following clean air by gasoline concentration sensor 212 being set on discharge pipe 12a, can discharging gasoline concentration usually, processing, the retracting device of safe gas-state hydrocarbon can be provided.Regularly switch adsorption- desorption tower 2,3 in addition and with the utilization of switching adsorption- desorption towers 2,3 and explanation in embodiment 1 by this gasoline concentration sensor 212, processing, the retracting device of safer gas-state hydrocarbon can be provided.Promptly, also can switch with 212 controls of gasoline concentration sensor on the main body, monitor gas circulation in advance with running cumulative time of air blast 4, even the occasion of also not switching in the setting value that reaches regulation judges that gasoline concentration sensor 212 switches unusually then.Perhaps utilize the running cumulative time control of pump 8 to switch on the main body, in advance with the gasoline concentration in the gasoline concentration sensor 212 monitoring discharge gases, even reach the occasion that regulation gasoline concentration is not also switched, can judge that also performance of the adsorbent switches unusually then.
[embodiment 12]
Figure 21 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 12.
In embodiment 7, show by making cold medium flow through heat exchanger 203 from refrigerator 201, make the medium temperature cooling of accumulating in the medium temperature groove 204 that has possessed heat exchange 203, the medium temperature of cooling is supplied with the situation of adsorption- desorption tower 2,3 by liquid circulation pump 202, and present embodiment is to discharge side at the medium temperature of liquid circulation pump 202 thermometer 213 that thermistor (temperature) sensor such as thermocouple constitutes is set, by this thermometer 213, the situation of the running of control refrigerator 203.Thus, the temperature of adsorption- desorption tower 2,3 can be controlled more accurately, the petrol vapor quantity of discharging can be stablized from adsorption-desorption tower 2,3.So, processing, the retracting device of safer gas-state hydrocarbon can be provided.
In addition, discharge the occasion that side is provided with thermometer 213, thermometer 213 need be made blast resistance construction at the medium temperature of liquid circulation pump 202.Therefore, the pipe arrangement that medium temperature is flowed extends up to the top with respect to ventilation voids 301, also can thermometer 213 be set at the position of also going up than ventilation voids 301.Thus, just there is no need thermometer 213 is made blast resistance construction, have the cheap effect of cost that can make device integral body.
In addition, having put down in writing said temperature meter 213 is situations of thermistor (temperature) sensors such as thermocouple, also can use bellows sensor (not illustrating among the figure) on thermometer 213.Usually, the bellows sensor by enclose liquid or gas in the inside of the temperature sensing tube of sense temperature, by bellows (lantern shapes of containers) that stretches with the detected volumetric expansion that causes by temperature of temperature sensing tube and the microswitch formation that stretches contact by bellows.If bellows sensor, can be detained the place at the flammable steam of ventilation voids 301 bottoms temperature sensing tube portion only is set, and bellows and microswitch are set at non-explosion-proof area, so there is no need thermometer 213 integral body are made blast resistance construction, have to make the whole cheap effect of cost is set.
Further, do not illustrate among the figure, but also can implement to supply to the medium temperature of adsorption- desorption tower 2,3 and the medium temperature of discharging,, detect the unusual such control in the adsorption- desorption tower 2,3 by its temperature difference from adsorption- desorption tower 2,3 with thermometer 213 monitorings.Thus, can provide safe retracting device.
[embodiment 13]
Figure 22 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 13.
In embodiment 7, show and receive oil supply as the oil supply signal according to the switch motion of giving oil nozzle 1 and begin situation with stop signal, and in the present embodiment, between to oil nozzle 1 and pump 8, pressure-regulating valve 214 and filter 215 are set in advance, the occasion of gas circulation blower 4 and pump 8 of turning round at the same time makes the gas of the regulation flow that flows in the pump 8 in advance, according to giving the take action of oil nozzle 1, receive oil supply and begin and stop signal from oil feeder.
Thus, even under the state of not sucking gasoline vapor for oil nozzle 1, also can turn round simultaneously gas circulation air blast 4 and pump 8, also can be corresponding simply for the occasion that enforcement intermittently carries out oil supply for the switch of oil nozzle 1.In addition, even leave the not state of oil supply from oil feeder for oil nozzle 1, processing, the retracting device of this gas-state hydrocarbon also turn round, owing to also turn round at the state retracting device that does not suck gasoline vapor, so from saving the viewpoint existing problems of the energy.Therefore, if such state continuance certain hour must carry in advance and stops the such controlling organization of retracting device.
As mentioned above, by between to oil nozzle 1 and pump 8, pressure-regulating valve 214 and filter 215 being set, according to giving the take action of oil nozzle 1 from oil feeder, receiving oil supply begins and stop signal, the processing of gas-state hydrocarbon, the running action of retracting device can be simplified, the cost of controlling organization can be reduced.
[embodiment 14]
Figure 23 and Figure 24 are all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiment of the present invention 14.
In the embodiment 7, show and when the gasoline vapor desorb, utilize mass flow controller B13a, B13b control supplies to the situation of the purified gas scale of construction in the desorber 3, present embodiment as shown in figure 23, be that the constant current valve B101a that has only certain gas flow to flow through is set, B101b and valve B102a, B102b flow through the mode of setting flow.In addition, as shown in figure 24, the pressure that also can be provided with in the desorber 3 is the such constant pressure valve B103a of setting pressure, B103b and valve B102a, and the pressure when B102b makes desorb in the desorber 3 is for certain.
As above-mentioned, by being used in combination valve B102a, B102b and constant flow rate valve B101a, B101b or constant pressure valve B103a, B103b does not use the mass flow controller B13a of high price, and B13b can provide processing, the retracting device of cheap gas-state hydrocarbon.
[embodiment 15]
Figure 25 and Figure 26 are all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiment of the present invention 15.
In the embodiment 14, show being used in combination valve B102a, B102b and constant flow rate valve B101a when the gasoline vapor desorb, B101b or constant pressure valve B103a, B103b, control supplies to the situation of the purified gas scale of construction in the desorber 3, and present embodiment is as shown in figure 25, be by changing the gasoline vapor pipe arrangement, by valve B102a, one of two of B102b and constant pressure valve B101, making flows in the desorber 3 sets the mode of flow.In addition, as shown in figure 26, also can pass through to change the gasoline vapor pipe arrangement, by using valve B102a, one of two of B102b and constant pressure valve B103, the pressure when making desorb in the desorber 3 are certain.
As described above, by changing the gasoline vapor pipe arrangement, be used in combination valve B102a, B102b, with constant flow rate valve B101 or constant pressure valve B103, reduce the use amount of constant flow rate valve B101 or constant pressure valve B103, can seek the cost degradation of system, processing, the retracting device of the gas-state hydrocarbon of cheapness can be provided.
[embodiment 16]
Figure 27 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiment of the present invention 16.
In the embodiment 7, show by liquid circulation pump 202 and will be supplied to the temperature controlled situation of implementing adsorption- desorption tower 2,3 in the adsorption- desorption tower 2,3 by the medium temperature that temperature has been controlled, the temperature sensor 216 of the temperature of measuring adsorbent is set in adsorption- desorption tower 2,3 in the present embodiment, and the running of control liquid circulation pump 202 makes adsorbent reach design temperature.Thus, can reduce the energy of liquid circulation pump 202 consumption, processing, the retracting device of the little gas-state hydrocarbon of operating cost can be provided.In addition, as the installation site of temperature sensor 216, preferably the supply side at the gasoline vapor of adsorption- desorption tower 2,3 is equipped with.This position is because the most violent to the adsorption-desorption of the gasoline vapor of adsorbent, and it is big that the variations in temperature of adsorbent becomes, and can carry out the temperature control according to variations in temperature fast.
In addition,, can confirm that whether adsorption-desorption operate security implementation, can improve the processing of gas-state hydrocarbon, the security of retracting device by the variations in temperature of temperature sensor 216 monitoring adsorption- desorption towers 2,3 is set.
As described above,, operating cost can be reduced, safer running can be realized simultaneously by the temperature sensor 216 of the temperature of measuring the adsorbent in the adsorption- desorption tower 2,3 is set.
[embodiment 17]
Figure 28 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 17.
Turn round simultaneously gas circulation air blast 4 and pump 8 have been shown in the embodiment 7, at adsorption tower 2 pressurization absorbing gasoline steams, occasion at desorber 3 decompression desorb gasoline vapors, in the present embodiment, with the suction side of air blast 4 pressure sensor 217 is set respectively in the exhaust side of pump 8 and gas circulation.Thus, can monitor the pressure of exhaust side of pump 8 and gas circulation pressure, can confirm that gas circulation is with air blast 4 and pump 8 regular event whether with the suction side of air blast 4.
Like this, by in the exhaust side of pump 8 and gas circulation with the suction side of air blast 4 design pressure sensor 217 respectively, can monitor the pressure of gasoline vapor flow line often, processing, the retracting device of safe gas-state hydrocarbon can be provided.
In the above description, show in the exhaust side of pump 8 and gas circulation and the occasion of pressure sensor 217 is set respectively, as shown in figure 29, also pressure sensor 217 can be installed in respectively on the adsorption- desorption tower 2,3 with the suction side of air blast 4.Thus, the pressure that can monitor in the adsorption- desorption tower 2,3 are pressurization or decompression, can confirm that gas circulation is with air blast 4 and pump 8 regular event whether.In addition,, also can confirm valve B11a in this occasion, B11b, B12a, B12b, B14a, whether B14b, mass flow controller B13a, B13b regular event.
As described above,, can monitor the pressure in the adsorption- desorption tower 2,3 often, processing, the retracting device of safer gas-state hydrocarbon can be provided by at adsorption- desorption tower 2,3 pressure sensor 217 being set respectively.
[embodiment 18]
Figure 30 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 18.
Illustrated in the embodiment 7 by pump 8 and will directly supply with the occasion of condensing unit 6 from the gasoline vapor of sucking for oil nozzle 1, present embodiment is the exhaust side branch gas line at pump 8, gas line 218 by condensing unit 6 is set, the mode of valve B104 and B105 is set at pipeline separately.Thus, even in the occasion of supplying with from pump 8 than the also low low temperature gasoline vapor of the design temperature of condensing unit 6, the moisture that also can prevent to be contained in condensing unit 6 in the gasoline vapor freezes, and pipe arrangement is jammed in possible trouble, can stablize the recovery of carrying out gasoline vapor.In addition, as the mensuration position of temperature, can consider gasoline vapor flow line and extraneous gas.
In this occasion, also can monitor temperature in advance by the gasoline vapor of pump 8, under this temperature, operate valve B104 and B105, also can monitor the temperature of extraneous gas, operation valve B104 and B105 under this temperature.But when attracting gasoline vapor for oil nozzle 1, extraneous gas also enters, so follow the extraneous gas temperature owing to contain the temperature of the air of gasoline vapor, promptly uses the control of extraneous gas temperature also can obtain effect of sufficient.In addition, because the extraneous gas temperature sharply do not change, thus can stable operation valve B104 and B105, also can control easily in the system.
Like this, by exhaust side branch gas line at pump 8, the gas line 218 by condensing unit 6 is set, at separately pipeline valve B104 and B105 are set, can prevent that pipe arrangement is jammed in possible trouble in the condensing unit 6, processing, the retracting device of safe gas-state hydrocarbon can be provided.
[embodiment 19]
Figure 31 is the key diagram of structure of the adsorption-desorption tower of expression embodiment of the present invention 19.
In the embodiment 7, show the external structure of adsorption- desorption tower 2,3 is made cylindrical structure, at internal configurations fin-tube heat exchanger 22, between the aluminium fin, clog the independent silica gel 21 or the situation of synthetic zeolite or their mixture, present embodiment is that a plurality of cylindrical duct 31 are disposed side by side, independent silica gel 21 or synthetic zeolite or their mixture of filling in its cylindrical duct 31, the formation of flowing temperature medium around cylindrical duct 31.Thus, can homogeneous cooling drums pipe independent silica gel 21 or synthetic zeolite or their mixture in 31, can stably adsorb and remove gasoline vapor.
This occasion, such shown in figure 32, the section of cutting apart adsorption- desorption tower 2,3 with a plurality of hexagons 32, cylindrical duct 31 is set is connected to this hexagon 32 in making, by layout circle bobbin 31 very well-behavedly in adsorption tower 2,3, can in adsorption- desorption tower 2,3, fill independent silica gel 21 or synthetic zeolite or their mixture efficiently, and in whole cylindrical duct 31, can homogeneous cooling drums pipe 31 interior independent silica gel 21 or synthetic zeolite or their mixtures.In addition, do not illustrate in the drawings,, can prevent from underfeed to the adsorption-desorption tower medium temperature short- circuit flow 2,3 yet at the outer setting baffle plate of cylindrical duct 31.
As described above, insert many cylindrical duct 31 in the adsorption- desorption tower 2,3 by being formed in, the such structure of outer wall flowing temperature medium in this cylindrical duct 31 can cool off adsorbent, processing, the retracting device that can provide gasoline to remove the gas-state hydrocarbon of stable performance more equably.
[embodiment 20]
Figure 33 is the processing of the gas-state hydrocarbon of expression embodiment of the present invention 20, the outside drawing of retracting device.Like this, it is such that frame 33 can be set, and also can change the position of pipe arrangement and valve.Thus, do not need to be arranged on the set service apparatus frame of gasoline service station, can this retracting device be set in the space that service apparatus frame is set, so can save the space of gasoline service station.
As described above, service apparatus frame can be cancelled so that frame 33 can be set in the position by changing pipe arrangement and valve, and processing, the retracting device of gas-state hydrocarbon can be set in this space, can guarantee to vacate the space of gas station.
[embodiment 21]
Figure 34 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 21.
In embodiment 1, show and possess 2,3 liang of towers of adsorption-desorption tower, the adsorption- desorption tower 2,3 that makes its two tower as adsorption tower 2 and desorber 3 with separately function action, mutual its action of switching, carry out the situation of adsorption-desorption operation, in the present embodiment, only design 2 one towers of adsorption-desorption tower.The 219th, the dry air that is used for dry air is supplied with adsorption-desorption tower 2 generates machine, and the 220th, temporarily store the gas storagetank of the gasoline vapor of desorb, B106, B107, B108 are valves.
Next, the absorption action for gasoline vapor describes.If gasoline service station begins oil supply, valve B1, B11, B12, B106, B108 opens, running pump 8 and gas circulation suck from the gasoline vapor (normal temperature is about 40vol% down) of leaking for oil nozzle 1 with air blast 4 runnings, for example are pressurized in the condensing unit 6 of supplying gas about 0.3MPa.At this moment, in the condensing unit 6 that possesses in the medium temperature groove 204, if the heat exchanger 203 of cold medium in refrigerator 201 supplies to medium temperature groove 204, pass through medium temperature, remain on indirectly about 0 ℃-5 ℃, gasoline and be contained in moisture part condensation in the gas is separated into gas (gasoline vapor) and liquid (gasoline) by gas-liquid separator 9.The downside of condensing unit 6 is stayed in the liquid storage, and in liquid gasoline recover 5, gas is discharged from condensing unit 6 as liquids recovery.At this moment, gas circulation also turns round with air blast 4, attracts gasoline vapor by valve B108 from gas retention basin 220, and the pressure in the gas retention basin 220 reduces.If the pressure of gas retention basin 220 reaches setting, shut off valve B108 stops gas circulation air blast 4.On the other hand, the gasoline vapor about the 10vol% that can not handle in condensing unit 6 is supplied gas and is handled in the adsorption-desorption tower 2, and gasoline vapor becomes pure air in the adsorption-desorption tower, is released in the atmosphere by pressure controller 120.
Next, describe for the desorb action.After the random time adsorption treatment, pump 8 stops in adsorption-desorption tower 2, valve B1, and B11, B12, B106, B108 closes, the beginning desorb.Thereafter, open valve B14, B107, the running gas circulation is attracted desorb with air blast 4 from adsorption-desorption tower 2 gasoline vapors.The gasoline vapor of discharging from adsorption-desorption tower 2 supplies to gas retention basin 220 by gas circulation with air blast 4.If the pressure in the adsorption-desorption tower 2 reaches setting, the running dry air generates machine 219, with certain flow dry air is supplied in the adsorption-desorption tower, by the gas purification of dry air, promotes the desorb of gasoline vapor.Thereafter, if the pressure of gas retention basin 220 reaches setting, shut off valve B14 and B108 stop gas circulation and generate machine 219 with air blast 4 and dry air.Like this, the moment in that the gasoline desorb finishes, be re-used as the adsorption tower utilization, move with this repeatedly in time.By such action, the gasoline in the recovery gasoline vapor that can liquefy makes gasoline concentration often discharge at 1vol% or following pure air simultaneously.But owing to need adsorption-desorption action repeatedly in time, so be difficult to be useful in the occasion of continuous processing gasoline vapor.
More than in the explanation, be described for the occasion that possesses dry air generation machine 219, by improving the ability of gas circulation with air blast 4, generate machine 219 even without dry air, also can liquefy and reclaim gasoline in the gasoline vapor, simultaneously, can often discharge gasoline concentration is 1vol% or following clean air.
As described above, in the present embodiment, by making adsorption-desorption tower 2 is a tower, gas retention basin 220 is set, there is no need to switch the control of adsorption-desorption tower 2, simultaneously, can reduce the cost of adsorption-desorption tower 2, processing, the retracting device of simple, the cheap gas-state hydrocarbon of control can be provided.
[embodiment 22]
Figure 35 is all pie graphs of flow process of processing, retracting device of the gas-state hydrocarbon of expression embodiments of the present invention 22.
In embodiment 7, show gasoline concentration and be 1vol% or following pure air and be discharged to situation in the atmosphere by pressure controller 120, present embodiment is to set in advance fire extinguisher 221 in the downstream of pressure controller 120, even in the occasion of flaring up from the outside, fire can not arrive inner mode yet.Thus, can prevent that outside fire from invading innerly, processing, the retracting device of safer gas-state hydrocarbon can be provided.In addition, do not illustrate in the drawings, on the pipeline that the liquified petroleum of discharging from liquified petroleum recover 5 flows, fire extinguisher 221 is set also, can obtain same effect yet.
Claims (2)
1. the processing of gas-state hydrocarbon, recovery method, it is characterized in that, possess the condensing unit of removing moisture and gasoline vapor, in the means that have adsorption tower and the more than one adsorption-desorption device of desorber and cool off this adsorption-desorption device of the gas downstream side design of this condensing unit, as adsorbent, use independent silica gel or synthetic zeolite or its mixture of aperture 4-100 dust, carry out adsorption-desorption, further the part of the exit gas of adsorption tower is delivered in the desorber Purge gas of the part of the discharge gas when using absorption during as desorb.
2. the processing of the described gas-state hydrocarbon of claim 1, recovery method is characterized in that, begin to import Purge gas when the internal pressure of aforementioned desorber reaches authorized pressure.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2004371996 | 2004-12-22 | ||
| JP2004371996 | 2004-12-22 | ||
| JP2005170999 | 2005-06-10 | ||
| JP2005170999A JP4671772B2 (en) | 2004-12-22 | 2005-06-10 | Apparatus and method for treating and recovering gaseous hydrocarbons |
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| CNB2005101381389A Division CN100354393C (en) | 2004-12-22 | 2005-12-22 | Apparatus and method for processing and recovering gaseous hydrocarbons |
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| CN101121093A CN101121093A (en) | 2008-02-13 |
| CN100584431C true CN100584431C (en) | 2010-01-27 |
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| CN200710108900A Expired - Fee Related CN100584431C (en) | 2004-12-22 | 2005-12-22 | Method for treating and recovering gaseous hydrocarbon |
| CNB2005101381389A Expired - Fee Related CN100354393C (en) | 2004-12-22 | 2005-12-22 | Apparatus and method for processing and recovering gaseous hydrocarbons |
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| CNB2005101381389A Expired - Fee Related CN100354393C (en) | 2004-12-22 | 2005-12-22 | Apparatus and method for processing and recovering gaseous hydrocarbons |
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| Country | Link |
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| JP (1) | JP4671772B2 (en) |
| KR (2) | KR100728451B1 (en) |
| CN (2) | CN100584431C (en) |
| TW (1) | TW200626709A (en) |
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- 2005-12-08 KR KR1020050119362A patent/KR100728451B1/en active Active
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Also Published As
| Publication number | Publication date |
|---|---|
| KR100815720B1 (en) | 2008-03-20 |
| TW200626709A (en) | 2006-08-01 |
| CN101121093A (en) | 2008-02-13 |
| CN1807555A (en) | 2006-07-26 |
| KR20060071872A (en) | 2006-06-27 |
| KR100728451B1 (en) | 2007-06-13 |
| HK1116442A1 (en) | 2008-12-24 |
| TWI310785B (en) | 2009-06-11 |
| HK1095353A1 (en) | 2007-05-04 |
| CN100354393C (en) | 2007-12-12 |
| JP4671772B2 (en) | 2011-04-20 |
| KR20070053671A (en) | 2007-05-25 |
| JP2006198604A (en) | 2006-08-03 |
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