CN100354393C - Treatment, retracting device and method for gas-state hydrocarbon - Google Patents
Treatment, retracting device and method for gas-state hydrocarbon Download PDFInfo
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- CN100354393C CN100354393C CNB2005101381389A CN200510138138A CN100354393C CN 100354393 C CN100354393 C CN 100354393C CN B2005101381389 A CNB2005101381389 A CN B2005101381389A CN 200510138138 A CN200510138138 A CN 200510138138A CN 100354393 C CN100354393 C CN 100354393C
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Classifications
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- 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)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Loading And Unloading Of Fuel Tanks Or Ships (AREA)
Abstract
To provide a small-sized and inexpensive treatment/recovery apparatus and a method of gaseous hydrocarbon preventing an adsorbent from being poisoned by moisture contained in gasoline vapor. This treatment/recovery apparatus is provided with a device recovering gasoline vapor leaking from a refueling nozzle 1 at refueling, a condensing apparatus 6 removing moisture contained in the gasoline vapor and gasoline vapor, and adsorbing/desorbing apparatuses 2, 3 of gasoline vapor provided in the downstream of gas in the rear stage of the condensing apparatus 6. During refueling, gasoline vapor is supplied to the condensing apparatus 6 and adsorbing/desorbing apparatus 2, gasoline vapor is released from the adsorbing/desorbing apparatus 3 synchronizingly with the action, and the desorbed gas is returned to the condensing apparatus to be treated.
Description
Technical field
The present invention relates to be released to processing, retrieving arrangement and the method for gas-state hydrocarbon contained in the atmospheric gas, 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 vent pipe by the waste exhaust gases induction pipe adsorption tower of supplying gas by gas blower (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 vacuum pump by the purge gas induction pipe.As purge gas, use the part of the Purge gas of when the absorption running, discharging from the adsorption tower top, vacuum pump turns round under about 25Torr.
The Purge gas that contains gasoline vapor after the desorb is supplied gas by induction pipe in the gasoline withdrawer, contacts with liquid gasoline by distribution piping, as the gasoline vapor in liquid (gasoline absorption liquid) the reclaiming clean waste gas.
In waste exhaust gases from the gasoline withdrawer, 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 topsoil.
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 vacuum 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 sorbent material 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 sorbent material 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, retrieving arrangement and method that sorbent material 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, retrieving arrangement possess the condensing works 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 works.
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 desorption tower at least, means with this adsorption-desorption device of cooling, as sorbent material, 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 desorption tower, the gas when using desorb is as Purge gas.
The present invention removes the condensing works 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 retrieving arrangement.Especially,, do not worry that sorbent material is poisoned by moisture yet, in the pipe arrangement of condensing works 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 certain temperature, and the temperature of control condensing works and adsorption-desorption device is compared with occasion of each device of control respectively, can make the pilot 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 vapor-recovery unit of energy.Have again,, can also can reduce the usage quantity of sorbent material with a large amount of gasoline vapor of quite few adsorbents adsorb in order to cool off adsorption tower.
Further, can obtain following unusual effect: the unusual temperature that can suppress in the adsorption tower that heat of adsorption brings rises, and makes the temperature homogenization in the adsorption unit, security that can very relieved adsorption unit.
The simple declaration of accompanying drawing
Fig. 1 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 1, and expression is provided with the example of 1 condensing works.
Fig. 2 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 1, and expression is provided with the example of the 1st condensing works and the 2nd condensing works.
Fig. 3 is with the oblique drawing shown in in-built a part of otch of the adsorption-desorption tower of Fig. 1, Fig. 2.
Fig. 4 is the performance chart 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, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 2.
Fig. 6 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 3.
Fig. 7 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 4.
Fig. 8 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 5.
Fig. 9 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 6.
Figure 10 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 7.
Figure 11 is the pie graph of layout of processing, retrieving arrangement of the gas-state hydrocarbon of expression Figure 10.
Figure 12 is with the oblique drawing shown in in-built a part of otch of the adsorption-desorption tower of Figure 10.
Figure 13 is the performance chart 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 chart of the relation of the gasoline concentration of discharging from the adsorption-desorption tower.
Figure 15 is used to illustrate adsorption-desorption tower internal pressure and the gasoline concentration of discharging from adsorption-desorption tower expellant gas flow, from the adsorption-desorption tower and the performance chart of the relation of 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 works reclaims the performance chart of the relation of flow.
Figure 17 carries out the oblique drawing 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, retrieving arrangement.
Figure 18 is the processing of the gas-state hydrocarbon of expression embodiments of the present invention 9, the gas circulation gas blower and the pump structure figure of retrieving arrangement.
Figure 19 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 10.
Figure 20 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 11.
Figure 21 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 12.
Figure 22 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 13.
Figure 23 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 14.
Figure 24 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 14.
Figure 25 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 15.
Figure 26 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 1.
Figure 27 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 16.
Figure 28 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 17.
Figure 29 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 17.
Figure 30 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 18.
Figure 31 is that the in-built part of desorption tower of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 19 is carried out the oblique drawing 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, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 20.
Figure 34 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 21.
Figure 35 is all pie graphs of flow process of processing, retrieving arrangement 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 gas blower (pump), 5 liquified petroleum withdrawers, 6 condensing workss, 7 the 2nd condensing workss, 8 pumps, 9 gas-liquid separators, 11 waste exhaust gases induction pipes, 12a, the 12b vent pipe, 13a, 13b Purge gas induction pipe, 14a, Purge gas induction pipe after the 14b desorb, 21 silica gel, 22 fin-tube heat exchangers, 41 pressure warning units, 120a, the 120b pressure controller, 201 refrigerators, 202 liquid circulating pumps, 203 heat exchangers, 204 medium temperature grooves, 205 auxiliary temperature media slot, 211 injectors, 212 gasoline concentration sensors, 213 thermometers, 214 pressure regulator valves, 215 strainers, 216 temperature sensors, 217 pressure transmitters, 218 gas tubes, 219 dry airs generate machine, 220 gas retention basins, 221 flash arrestors, 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 gangway, R5, R6 hot gas gangway, H1, the H2 well heater
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 retrieving arrangement flow process, and Fig. 1 has represented to design the example of 1 condensing works, and Fig. 2 has represented to design the example of the 1st condensing works and the 2nd condensing works.Fig. 3 is the oblique drawing of expression with the internal structure part otch of the adsorption-desorption tower of Fig. 1, Fig. 2, and Fig. 4 is the performance chart 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 works (being the 1st condensing works among Fig. 2), 7 is the 2nd condensing workss, the 9th, and gas-liquid separator, the 5th, liquified petroleum withdrawer, 2, the 3rd, as the adsorption-desorption tower of adsorption-desorption device, the 4th, gas circulation gas blower (pump).B1 is to the valve that is closing beyond the 1 oil supply time of oil nozzle, the 11st, gasoline vapor induction pipe, B11a that condensing works 6 or the 1st, the 2nd condensing works 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 induction pipe 11,12a, 12b be provided in a side of adsorption- desorption tower 2,3 the top to atmospheric vent pipe, 120a, 120b are arranged on the pressure controller on this vent pipe 12a, the 12b.
In addition, 13a, 13b are the Purge gas induction pipes, be used for and deliver to desorption tower 3 or 2 from the part that adsorption tower 2,3 is discharged to atmospheric clean air as Purge gas, B13a, B13b are arranged on the mass flow controller of the pilot-gas amount on this Purge gas induction pipe 13a, the 13b, 14a, 14b are the Purge gas blast tubes 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 blast tube 14a, the 14b smokes valve.R1, R2 are the entrance and exits of the cold medium of discrepancy condensing works 6, R3, R4 are the entrance and exits of the more cryogenic cold medium of discrepancy the 2nd condensing works 7, 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 warning unit of gas circulation with the exhaust side of gas blower 4.
Next, the processing of the gas-state hydrocarbon of Fig. 1, the action of retrieving arrangement are described.When the service 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 works 6.The inside of condensing works 6 makes it be passed to outlet R2 by making cold medium from going into the R1 importing, 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 works 6 is stayed in the liquid storage, in liquified petroleum withdrawer 5, gas is discharged from condensing works 6 as liquids recovery.Import gasoline vapor by the top from condensing works 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 10Vol% under the operating condition 0.3MPa of condensing works 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 works 7 thereafter.This situation is as follows.
Next, the gasoline vapor about the 10Vol% that the 1st condensing works 6 fails to handle is supplied gas and is handled in the 2nd condensing works 7.In the 2nd condensing works 7, by importing from inlet R3 than the more cryogenic cold medium of the 1st condensing works 6 to outlet R4 circulation, such the 2nd condensing works 7 is set in more low temperature, for example-10 ℃ about.In the 2nd condensing works 7, gasoline and moisture and the 6 same condensations of the 1st condensing works are reclaimed.Situation in temperature running below freezing is also arranged in the 2nd condensing works 7,, worry sometimes because the ice that produces in the 2nd condensing works 7 stops up the situation of the gas passage in the 2nd condensing works 7 according to the occasion difference.For fear of such problem, stop the circulation of cold medium at regular intervals, the cold medium of pyritous etc. that perhaps circulates, 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-losses is set in the 2nd condensing works 7, if the pressure-losses surpasses set(ting)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 works 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 works 7 ,-10 ℃ condition.This gasoline vapor is vented to processing in the adsorption-desorption tower 2,3.2 situations of moving as desorption tower as adsorption tower, 3 in Fig. 1, Fig. 2, have been provided.Therefore, valve B11a is an open state, and valve B11b is a closing condition.In adsorption tower 2, use as desorption tower 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 induction pipe 11 in the adsorption tower 2.Enclose the sorbent material of absorbing gasoline steam in the adsorption-desorption tower 2,3.As the sorbent material 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 sorbent material absorption by gasoline vapor and remove gasolene ingredient, becoming gasoline concentration is 1Vol% or following uncontaminated air, and 12a is released in the atmosphere by vent pipe.Adsorption tower 2 utilizes cryogenic cold medium or additive method to be cooled off by utilizing the 2nd condensing works 7, seeks to remove because heat that absorption produces and increase loading capacity.In addition, by reducing the temperature inside of adsorption tower 2, can increase loading capacity.
But, also lower if the internal temperature of adsorption tower 2 is reduced to than the design temperature of the 1st condensing works 6 or the 2nd condensing works 7, in order to make water condensation in adsorption tower 2,, preferably set in almost identical temperature with condensing works 6 in the occasion of having only condensing works 6.In addition, in the occasion that has the 2nd condensing works 7, preferably set into the design temperature of the 2nd condensing works 7.Further, on atmospheric vent pipe 12a, 12b, setting, making the pressure in the adsorption tower 20 maintain prescribed value pressure controller 120a, the 120b of pressure-controlling at prescribed value.In the occasion of Fig. 2 owing to use the waste exhaust gases of the high pressure (about 0.3MPa) of the 2nd condensing works 7 to adsorb, so can improve loading 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-level efficiency to adsorb, is effective at the partially filled fluorine class of the ventilating pit of fin-tube heat exchanger 22 packing material.In addition, for the space in the ventilating pit part does not flow into gasoline vapor, also can seal the space of ventilating pit 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 works 6 or the 1st, the 2nd condensing works 6,7 is not set, is contained in water adsorption in the gasoline vapor on sorbent material, the absorption property of gasoline vapor descends, and needs the above sorbent material 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 works 6 or the 1st, the 2nd condensing works 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 workss 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 density (40Vol%) that oil nozzle 1 reclaims at the 1st, 2 condensing workss 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 works 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 works 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 sorbent material uses gas blower 4 through gas from the sorbent material desorb gasoline of the attraction of the purified gas induction pipe 14a after the desorbs from desorption tower 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 sorbent material so utilize this pressure difference owing to reduce pressure below the normal atmosphere with gas blower 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 works 6.In the occasion of Fig. 2, turn back in the 2nd condensing works 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 works 7.
Only utilizing owing to the desorption method of gas circulation with the pressure difference of the attraction generation of gas blower 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 desorption tower 3 and use by vent pipe 12, Purge gas induction pipe 13a as the part that is discharged to the clean gas the atmosphere from adsorption tower 2 of this Purge gas.B1 3a, B1 3b 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 specified amount 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 volume also to reduce.Therefore, increase the Purge gas flow, prevent that it is effective attracting the reduction of gas volume.The interior unnecessary gas of the system of sending into causes the power homenergic loss of gas circulation with gas blower 4, so the flow control of preferred neat oxidizing gases is in the needs inferior limit.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 detrimentally affect of the sorbent material in the desorption tower 3 in the condensing works 6 or the 1st of adsorption- desorption tower 2,3 leading portions, the 2nd condensing works 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 change 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 of mobile, make temperature in the desorption tower 3 near room temperature from inlet R3b to outlet R4b at desorption tower 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 sorbent material does not spill so worry gasoline.Along with the process of time, the adsorptive capacity of gasoline increases, and the temperature of adsorption tower also reduces simultaneously, and the absorption property of sorbent material 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, increased the energy expenditure of refrigerator and well heater, thus 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 clipping time 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 works 6 discontinuous runnings.On the other hand, utilize gas circulation with the loop line circuit of gas blower 4, promptly, comprise that the system of the 2nd condensing works 7, adsorption- desorption tower 2,3 has adopted the formation of continuous operation.When the circuit internal recycle gas of this loop line, 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 gaseous tension 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 sorbent material.Perhaps a part of excessive pressure in the closed circuit rises to safe above base line, worries to follow pyrophoric danger.Therefore,, set pressure warning unit 41 in gas circulation with the exhaust side of gas blower 4 in advance,, stop gas circulation automatically, use such Security Countermeasures with gas blower 4 in the occasion of the pressure range that surpasses regulation in the occasion of Fig. 2.
[embodiment 2]
Fig. 5 is all pie graphs of flow process of processing, retrieving arrangement 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 desorption tower 3 desorbs the 1st condensing works 6.In the present embodiment, do not need the used gas circulation of Fig. 1 gas blower 4.But if intermitten pump 8 when oil supply only, according to the running-active status of pump 8, there is the situation that is difficult to adsorb control in the pressure change of adsorption-desorption tower 2,3.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, retrieving arrangement 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 use temperature.Externally gas introduction port-Purge gas induction pipe 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 sorbent material in the desorption tower 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, retrieving arrangement 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 difference, temperature head 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, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 5.
Present embodiment is to substitute cold medium in desorption tower 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, retrieving arrangement 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 induction pipe 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, retrieving arrangement of the gas-state hydrocarbon of expression embodiment of the present invention 7.
Present embodiment and embodiment 1 difference are, use refrigerator 201 cooling temperature media (salt solution liquid etc.), by liquid circulating pump 202 this medium temperature are supplied with condensing works 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 refrigerative medium temperature is supplied with condensing works 6 and adsorption- desorption tower 2,3 by liquid circulating 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 works 6 in medium temperature groove 204, supply with the example of adsorption- desorption tower 2,3 by liquid circulating 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 works, the 9th, gas-liquid separator, the 5th, liquified petroleum withdrawer, 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 gas blower, B1, connects gasoline vapor induction pipe, the B11a of condensing works 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 induction pipe 11.The 120th, the pressure controller of adjusting adsorption-desorption tower 2,3 pressure, 12a, 12b are the vent 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 vent 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 desorption tower 3 or 2 and the Purge gas induction pipe, the B13a that use as Purge gas, and B13b is arranged on the mass flow controller of the pilot-gas flow on this purge gas induction pipe 13a, the 13b.
14a, 14b connects gas circulation blower 4 and adsorption-desorption tower 2, Purge gas blast tube after 3 the desorb, B14a, B14b is arranged on this Purge gas blast tube 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, 2 02 is to supply with adsorption-desorption tower 2 by refrigerator 201 refrigerative medium temperatures, 3 liquid circulating 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 heat exchanger 203 refrigerative medium temperatures.
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 retrieving arrangement 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 works 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 explosion-proof structure in order to ensure security.
In addition, liquid circulating 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 circulating pump 202 is arranged on the top of ventilation voids 301, liquid circulating 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 circulating pump 202, worry to produce the problem that to cool off adsorption-desorption tower 2,3.Therefore, making the liquid circulating pump 202 of explosion-proof structure 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 power of device, so safer retrieving arrangement can be provided.
Next, action is described.When the service 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 works 6.If the condensing works 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 works 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 works 6 is stayed in the liquid storage, in liquified petroleum withdrawer 5, gas is discharged from condensing works 6 as liquids recovery.Import gasoline vapor by the top from condensing works 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 cooling temperatures, gas flow 60L/min at the operating condition of condensing works 6.In addition, as from the saturation concentration graphic representation 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 works 6.But, if the water that design temperature below freezing, is contained in the gas freezes in condensing works 6, the pipe arrangement blocking problem can take place, so the design temperature of condensing works 6 is preferably about 0 ℃-5 ℃.
Next, the gasoline vapor about the 10Vol% that will fail to handle in condensing works 6 is supplied gas and is handled in the adsorption-desorption tower 2,3.Figure 10 illustrates 2 situations when moving as desorption tower as adsorption tower, 3.Therefore, valve B11a open (painting black), B11b (not having blacking, barren) is a closing condition.Adsorption tower 2 uses as desorption tower 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 switching valve B11a, B11b controls as described above in the switching of absorption, desorb.
Gasoline vapor is supplied gas by induction pipe 11 in the adsorption tower 2.Enclose the sorbent material of absorbing gasoline steam in the adsorption-desorption tower 2,3.As the sorbent material 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 sorbent material, become gasoline concentration 1Vol% or following uncontaminated air, 12a is released in the atmosphere by vent pipe.To atmospheric vent pipe 12a, the downstream side of 12b sets the pressure controller 120 of control pressure at prescribed value, so that the pressure in the adsorption tower 2 are maintained prescribed value.In the present embodiment,, can improve loading capacity significantly than absorption under normal pressure owing to use the waste exhaust gases absorption of the high pressure (about 0.3MPa) of condensing works 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 certain temperature by the medium temperature of being supplied with by liquid circulating pump 202.That is, usually the cooling system of running control condensing works 6 and adsorption- desorption tower 2,3 makes it maintain design temperature.This is that be absolutely necessary cooling 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 power in the short period of time cooling brings bad influence.Have again,, can increase loading capacity, reduce the usage quantity 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 works 6, water condensation in adsorption tower 2 is further frozen in occasion below freezing, so preferably set in the temperature almost same with condensing works 6.
From the above fact, maintain the temperature of setting for the cooling system that makes condensing works 6 and adsorption- desorption tower 2,3, and for the pressure system that makes condensing works 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, itself and gasoline vapor mobile direction are 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 ventilating pit one side, be provided with and partly contact such reticulation or tabular metal (aluminium or the copper of heat transfer characteristic excellence are the most suitable) with ventilating pit, there be not ventilating pit 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 can make medium temperature mobile pipe arrangement branch before entering heat-transfer pipe in the heat-transfer pipe of fin-tube heat exchanger 22, and fin-tube heat exchanger 22 is divided into multistage, and medium temperature is flowed side by side.Thus, the pressure-losses of medium temperature mobile pipe arrangement can be reduced, the capacity of medium temperature being supplied with the liquid circulating 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 works 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 sorbent material, the absorption property of gasoline vapor descends, and needs the above sorbent material 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 works 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 works 6, can be reduced to 10Vol% from the gasoline of giving the high density (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 works 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 sorbent material uses gas blower 4 through gas from the strippant desorb gasoline of purified gas induction pipe 14a attraction from desorption tower 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 normal atmosphere with gas blower 4,, be adsorbed on gasoline on the sorbent material by desorb so utilize this pressure difference 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 works 6.In addition, during desorb, by rising desorption tower 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 well 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 supplying opening of adsorption tower 2 when the relief outlet of the gasoline vapor of the desorption tower 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 port near absorbing gasoline steam to high-density, gasoline vapor almost not have the state that adsorbs near the gasoline vapor relief outlet of adsorption tower 2.The gasoline vapor of discharging from desorption tower 3 during for high efficiente callback desorb in condensing works 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 density, 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 port of adsorption tower 2.
Only utilizing because in the desorption method of gas circulation with the pressure difference of the attraction generation of gas blower 4, its efficient is not too high, is effective so import Purge gas from the outside.In the present embodiment, as this Purge gas, the part that will be discharged to atmospheric uncontaminated air from adsorption tower 2 is sent pipe 13a by vent pipe 12a, Purge gas and is delivered to desorption tower 3 and use.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 specified amount 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 works 6, so the moisture that is contained in the Purge gas produces detrimentally affect to the sorbent material in the desorption tower 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 density as much as possible from desorption tower 3, this is the known fact.Further, send into unwanted gas and can cause gas circulation with the loss of the power homenergic of gas blower 4 in system, to need inferior limit 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 volume also to descend.Therefore, begin effectively to prevent to attract the reduction of gas volume 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 desorption tower 3 reaches set(ting)value, the gas volume of the gasoline vapor of discharging from desorption tower 3 imports the mode (gas volume instrumentation mode) of Purge gas when reaching set(ting)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 desorption tower 3, enough gasoline vapors being arranged, import Purge gas, reduced the gasoline vapor concentration of discharging thus from desorption tower 3 if adsorptive capacity is many.On the contrary, if adsorptive capacity is few, the time band that the gasoline vapor gas volume of discharging from desorption tower is few increases, and can not effectively eject the gasoline vapor from desorption tower 3.Pressure instrumentation mode and gas volume 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 gasoline vapor mobile piping system the setting pressure meter be integral.Therefore and since pressure instrumentation mode can with these pressure warning unit dual-purposes, so think in 3 kinds of modes the most effective.
Figure 14 represents from the pressure change 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 2 0NL/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 stabilized zone), and gasoline concentration slowly reduces thereafter.Therefore, as can be known in order in condensing works 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 works 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 gasoline vapor concentration of discharging from adsorption-desorption tower 2,3 expellant gas flows (Purge gas flow) with 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, the vent gas scale of construction (the purified gas scale of construction) in running as can be known.But in this retrieving arrangement, 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 works 6, need make in the expellant gas 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 threshold concentration the condensing works 6 is 10vol% from adsorption- desorption tower 2,3, with product representation from adsorption- desorption tower 2,3 expellant gas flows (Purge gas flow).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 works 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 works 6, just increases the gasoline vapor that moves to adsorption tower 2 from desorption tower 3, the cause that reduces as the running efficiency of retrieving arrangement.
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 desorption tower 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 desorption tower 3 be 4.5 NL/min or more than.Hence one can see that, need make internal pressure in the adsorption- desorption tower 2,3 at 1 5-4 0kPa.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 desorption tower 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 uncontaminated air in 1vol% or following gasoline concentration from adsorption tower 2,12a is released in the atmosphere by vent pipe.In this retrieving arrangement, in order to be used for from the air that adsorption tower 2 is discharged discharging gasoline from desorption tower 3, moving and move from the desorb of desorption tower 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 gas blower 4 in the same period.By such running, the gasoline vapor of desorb with the air dilution that gas blower 4 is inhaled into, can not occur the reduction of the organic efficiency of condensing works 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 desorption tower 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 gas blower 4 and reclaim.In addition, the running 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 uncontaminated air, and 12a is released in the atmosphere by vent pipe.But along with the petrol vapor quantity of supplying with in the adsorption tower 2 increases, the adsorptive power 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 retrieving arrangement.
Therefore, the switching of adsorption- desorption tower 2,3 is effective by the aggregate-value of gasoline recovery plant opening time.That is, can reach the moment of specified 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 runtime at first at the aggregate-value of gasoline recovery plant runtime.In addition, as the index of expression retrieving arrangement running, can enumerate the running of gas circulation with gas blower 4 or pump 8.In this device, because gas circulation is with gas blower 4 and running 8 same periods of pump, so tired to calculate which all no problem runtime.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 prescribed value 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 over-drastic pressure, safe gasoline recovery plant can be provided.
At last, the processing of gas-state hydrocarbon, the control method of retrieving arrangement are described.When retrieving arrangement stops, stopping gas circulation gas blower 4 and pump 8, valve B11a, B11b, B12a, B12b, B14a, B14b are full closing state, mass flow controller B13a, B13b are closing 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 gas blower 4 and pump 8.If with the running of gas blower 4, the pressure in the desorption tower 3 drop to normality by gas circulation, the beginning of mass flow controller B13a opened, and the aperture of controlling quality flow director B13a makes the flow of the regulation that flows in the desorption tower 3.After oil supply finishes, accept the stop signal from oil feeder, gas circulation stops with gas blower 4 and pump 8, and mass flow controller B13a becomes closing condition, valve B11a, and B12a, B14a becomes closing condition.
Like this, oil supply if the aggregate-value of oil supply time reaches the specified 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 specified time in the oil supply.If the stop signal of acceptance, then as previously mentioned, gas circulation stops with gas blower 4 and pump 8, and mass flow controller B13a becomes closing condition, valve B11a, and B12a, B14a becomes closing 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 gas blower 4 and pump 8 runnings thereafter, and adsorption tower 3 becomes the absorption action, and desorption tower 2 becomes the desorb action.If by the running of gas circulation with gas blower 4, when the pressure in the desorption tower 2 was reduced to normality, mass flow controller B13b began to open, the aperture of controlling quality flow director B13b makes the flow that flows and stipulate in the desorption tower 2.After oil supply finishes, accept the stop signal from oil feeder, gas circulation stops with gas blower 4 and pump 8, and mass flow controller B13b becomes closing condition, valve B11b, and B12b, B14b becomes closing condition.Thereafter, till the oil supply cumulative time reaches the specified 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, retrieving arrangement also can turn round, the retrieving arrangement 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 retrieving arrangement.
As described above, the processing of the gas-state hydrocarbon of present embodiment, retrieving arrangement be because combination condensing works 6 and adsorption- desorption tower 2,3, so even be only discharge maximum also only for the gasoline vapor of 1vol%, be processing, the retrieving arrangement 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 retrieving arrangement 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, retrieving arrangement 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 circulating pump 202 above ventilation voids 301.According to present embodiment, do not need liquid circulating pump used in Figure 11 202 is made explosion-proof structure.But in liquid circulating 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 circulating pump 202, can the runs steadily system.
As described above, in the present embodiment,, can make the expense cheapness of liquid circulating pump 202, the processing of gas-state hydrocarbon, the cost of retrieving arrangement are reduced owing to do not need liquid circulating pump 202 is made explosion-proof structure.
[embodiment 9]
Figure 18 be expression embodiments of the present invention 9 gas-state hydrocarbon processing, retrieving arrangement gas circulation with compressor and pump structure figure.
In the processing of the gas-state hydrocarbon of present embodiment, retrieving arrangement, because the gas circulation that turns round simultaneously is with gas blower 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 electric motor 10 can be reduced, processing, the retrieving arrangement of cheap gas-state hydrocarbon can be supplied with.
[embodiment 10]
Figure 19 is all pie graphs of flow process of processing, retrieving arrangement 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 vent pipe 12a, be released to the situation in the atmosphere, and on vent 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 retrieving arrangement of safer gas-state hydrocarbon can be provided thus.
[embodiment 11]
Figure 20 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 11.
In embodiment 7, show the aggregate-value of the runtime of having calculated gas circulation usefulness gas blower 4 or pump 8 in advance, its value has reached set(ting)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 vent pipe 12a, be provided with gasoline concentration sensor 212 in the present embodiment, output valve from its gasoline concentration sensor 212 reaches set(ting)value, and the occasion that stops at pump 8 is switched adsorption- desorption tower 2,3 then.Processing, the retrieving arrangement 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 absorption formula of the ultrared absorbed dose of about 3.3 mum wavelengths.
Like this, be 1vol% or following clean air by gasoline concentration sensor 212 being set on vent pipe 12a, can discharging gasoline concentration usually, processing, the retrieving arrangement 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 retrieving arrangement 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 gas blower 4, even the occasion of also not switching in the set(ting)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, retrieving arrangement 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 refrigerative medium temperature is supplied with the situation of adsorption- desorption tower 2,3 by liquid circulating pump 202, and present embodiment is to discharge side at the medium temperature of liquid circulating pump 202 thermometer 213 that thermistor (temperature) sensor such as thermopair 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 retrieving arrangement 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 explosion-proof structure at the medium temperature of liquid circulating pump 202.Therefore, medium temperature mobile pipe arrangement is extended 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 explosion-proof structure, 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 thermopair, also can use corrugated tube transmitter (not illustrating among the figure) on thermometer 213.Usually, the corrugated tube transmitter by enclose liquid or gas in the inside of the temperature sensing tube of sense temperature, by corrugated tube (lantern shapes of containers) that stretches with the detected volumetric expansion that causes by temperature of temperature sensing tube and the vernier switch formation that stretches contact by corrugated tube.If corrugated tube transmitter, can be detained the place at the flammable steam of ventilation voids 301 bottoms temperature sensing tube portion only is set, and corrugated tube and vernier switch are set at non-explosion-proof area, so there is no need thermometer 213 integral body are made explosion-proof structure, 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 head from adsorption- desorption tower 2,3 with thermometer 213 monitorings.Thus, can provide safe retrieving arrangement.
[embodiment 13]
Figure 22 is all pie graphs of flow process of processing, retrieving arrangement 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 regulator valve 214 and strainer 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 gas blower 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 retrieving arrangement of this gas-state hydrocarbon also turn round, owing to also turn round at the state retrieving arrangement 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 retrieving arrangement.
As mentioned above, by between to oil nozzle 1 and pump 8, pressure regulator valve 214 and strainer 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 retrieving arrangement 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, retrieving arrangement 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 desorption tower 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, shown in Fig. 24, the pressure that also can be provided with in the desorption tower 3 is the such constant pressure valve B103a of setting pressure, B103b and valve B102a, and the pressure when B102b makes desorb in the desorption tower 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 retrieving arrangement of cheap gas-state hydrocarbon.
[embodiment 15]
Figure 25 and Figure 26 are all pie graphs of flow process of processing, retrieving arrangement 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 desorption tower 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 desorption tower 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 desorption tower 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 usage quantity of constant flow rate valve B101 or constant pressure valve B103, can seek the cost degradation of system, processing, the retrieving arrangement of the gas-state hydrocarbon of cheapness can be provided.
[embodiment 16]
Figure 27 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiment of the present invention 16.
In the embodiment 7, show by liquid circulating 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 sorbent material is set in adsorption- desorption tower 2,3 in the present embodiment, and the running of controlled liq recycle pump 202 makes sorbent material reach design temperature.Thus, can reduce the energy of liquid circulating pump 202 consumption, processing, the retrieving arrangement 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 sorbent material, and it is big that the temperature variation of sorbent material becomes, and can carry out the temperature control according to temperature variation fast.
In addition,, can confirm that whether adsorption-desorption operate security implementation, can improve the processing of gas-state hydrocarbon, the security of retrieving arrangement by the temperature variation 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 sorbent material in the adsorption- desorption tower 2,3 is set.
[embodiment 17]
Figure 28 is all pie graphs of flow process of processing, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 17.
Turn round simultaneously gas circulation gas blower 4 and pump 8 have been shown in the embodiment 7, at adsorption tower 2 pressurization absorbing gasoline steams, occasion at desorption tower 3 decompression desorb gasoline vapors, in the present embodiment, with the suction side of gas blower 4 pressure transmitter 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 gas blower 4 and pump 8 regular event whether with the suction side of gas blower 4.
Like this, by in the exhaust side of pump 8 and gas circulation with the suction side of gas blower 4 design pressure transmitter 217 respectively, can monitor the pressure of gasoline vapor flow line often, processing, the retrieving arrangement 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 transmitter 217 is set respectively, as shown in figure 29, also pressure transmitter 217 can be installed in respectively on the adsorption- desorption tower 2,3 with the suction side of gas blower 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 gas blower 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 retrieving arrangement of safer gas-state hydrocarbon can be provided by at adsorption- desorption tower 2,3 pressure transmitter 217 being set respectively.
[embodiment 18]
Figure 30 is all pie graphs of flow process of processing, retrieving arrangement 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 works 6 from the gasoline vapor of sucking for oil nozzle 1, present embodiment is the exhaust side branch gas tube at pump 8, gas tube 218 by condensing works 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 works 6, the moisture that also can prevent to be contained in condensing works 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, operating valve B104 and B105 under this temperature also can monitor the temperature of extraneous gas, operating 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 tube at pump 8, the gas tube 218 by condensing works 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 works 6, processing, the retrieving arrangement of safe gas-state hydrocarbon can be provided.
[embodiment 19]
Figure 31 is the explanatory view 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 configuration 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 yield temperature medium around cylindrical duct 31.Thus, can homogeneous cooling drum 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 sexangles 32, cylindrical duct 31 is set is connected to this sexangle 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 drum 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 yield temperature medium in this cylindrical duct 31 can cool off sorbent material, processing, the retrieving arrangement 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 retrieving arrangement.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 retrieving arrangement 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 retrieving arrangement of gas-state hydrocarbon can be set in this space, can guarantee to vacate the space of service station.
[embodiment 21]
Figure 34 is all pie graphs of flow process of processing, retrieving arrangement 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 desorption tower 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, the gas storage groove of the gasoline vapor of temporary storage 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 gas blower 4 runnings, for example are pressurized in the condensing works 6 of supplying gas about 0.3MPa.At this moment, in the condensing works 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 works 6 is stayed in the liquid storage, and in liquid gasoline withdrawer 5, gas is discharged from condensing works 6 as liquids recovery.At this moment, gas circulation also turns round with gas blower 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 prescribed value, shut-off valve B108 stops gas circulation gas blower 4.On the other hand, the gasoline vapor about the 10vo1% that can not handle in condensing works 6 is supplied gas and is handled in the adsorption-desorption tower 2, and gasoline vapor becomes uncontaminated 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 gas blower 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 gas blower 4.If the pressure in the adsorption-desorption tower 2 reaches prescribed value, the running dry air generates machine 219, with certain flow dry air is supplied in the adsorption-desorption tower, by the gas sweetening of dry air, promotes the desorb of gasoline vapor.Thereafter, if the pressure of gas retention basin 220 reaches prescribed value, shut-off valve B14 and B108 stop gas circulation and generate machine 219 with gas blower 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 uncontaminated 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 gas blower 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 retrieving arrangement 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, retrieving arrangement of the gas-state hydrocarbon of expression embodiments of the present invention 22.
In embodiment 7, show gasoline concentration and be 1vol% or following uncontaminated air and be discharged to situation in the atmosphere by pressure controller 120, present embodiment is to set in advance flash arrestor 221 in the downstream side 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 retrieving arrangement of safer gas-state hydrocarbon can be provided.In addition, do not illustrate in the drawings, on the liquified petroleum mobile pipeline of discharging, flash arrestor 221 is set also, can obtain same effect yet from liquified petroleum withdrawer 5.
Claims (6)
1. the processing of the gas-state hydrocarbon of the gasoline vapor that leaks when being used to handle the gasoline oil supply, retrieving arrangement, it is characterized in that the adsorption-desorption device of the gasoline vapor that possess the condensing works of removing moisture and gasoline vapor, is provided with in the gas downstream side of this condensing works.
2. the processing of the described gas-state hydrocarbon of claim 1, retrieving arrangement is characterized in that, possess a plurality of aforementioned condensing workss, and the gasoline vapor that will can not handle in the 1st condensing works is being set at than handling in the 2nd low condensing works of the 1st condensing works temperature.
3. processing, the retrieving arrangement of claim 1 or 2 described gas-state hydrocarbons is characterized in that, aforementioned adsorption-desorption device possesses 2 towers, a tower is moved as desorption tower as adsorption tower, another tower, through predefined time the time, its function is exchanged, handle gasoline vapor.
4. the processing of the described gas-state hydrocarbon of claim 1, retrieving arrangement, it is characterized in that, device with the gasoline vapor that when nozzle reclaims oil supply, leaks, possesses the condensing works that the moisture that will be contained in this gasoline vapor and gasoline vapor are removed, adsorption-desorption device at the gasoline vapor of the gas downstream side of this condensing works, by gasoline vapor being supplied with the adsorption tower of aforementioned condensing works and aforementioned adsorption-desorption device at the time band that carries out oil supply, carry out the same period with this action, gasoline vapor is discharged from the desorption tower of aforementioned adsorption-desorption device, this desorption gas is turned back to condensing works.
5. processing, the retrieving arrangement of claim 1 or 4 described gas-state hydrocarbons, it is characterized in that, inside at aforementioned adsorption-desorption device is provided with fin-tube heat exchanger, and filling is as independent silica gel or synthetic zeolite or its mixture of the aperture 4-100 dust of sorbent material between the fin of this fin-tube heat exchanger.
6. processing, the retrieving arrangement of claim 1 or 4 described gas-state hydrocarbons is characterized in that, use to carry out temperature controlled medium temperature by freezing or refrigerating unit, and the temperature of aforementioned condensing works and adsorption-desorption device is controlled at almost equal temperature.
Applications Claiming Priority (4)
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| 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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| CN200710108900A Division CN100584431C (en) | 2004-12-22 | 2005-12-22 | Processing and recovery method of hydrocarbon gas |
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| CN100354393C true CN100354393C (en) | 2007-12-12 |
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| CN200710108900A Expired - Fee Related CN100584431C (en) | 2004-12-22 | 2005-12-22 | Processing and recovery method of hydrocarbon gas |
| CNB2005101381389A Expired - Fee Related CN100354393C (en) | 2004-12-22 | 2005-12-22 | Treatment, retracting device and method for gas-state hydrocarbon |
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| JP (1) | JP4671772B2 (en) |
| KR (2) | KR100728451B1 (en) |
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| KR100815720B1 (en) | 2008-03-20 |
| HK1116442A1 (en) | 2008-12-24 |
| KR20070053671A (en) | 2007-05-25 |
| CN101121093A (en) | 2008-02-13 |
| KR20060071872A (en) | 2006-06-27 |
| HK1095353A1 (en) | 2007-05-04 |
| CN1807555A (en) | 2006-07-26 |
| JP4671772B2 (en) | 2011-04-20 |
| TWI310785B (en) | 2009-06-11 |
| KR100728451B1 (en) | 2007-06-13 |
| CN100584431C (en) | 2010-01-27 |
| TW200626709A (en) | 2006-08-01 |
| JP2006198604A (en) | 2006-08-03 |
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