CN101927099A - Apparatus and method for recovering gaseous hydrocarbon - Google Patents
Apparatus and method for recovering gaseous hydrocarbon Download PDFInfo
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- CN101927099A CN101927099A CN2009102523050A CN200910252305A CN101927099A CN 101927099 A CN101927099 A CN 101927099A CN 2009102523050 A CN2009102523050 A CN 2009102523050A CN 200910252305 A CN200910252305 A CN 200910252305A CN 101927099 A CN101927099 A CN 101927099A
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- 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
- B01D53/04—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 with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/0075—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with heat exchanging
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/0093—Removing and treatment of non condensable gases
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- 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
- B01D53/002—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 condensation
-
- 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
- B01D53/30—Controlling by gas-analysis apparatus
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Treating Waste Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a recovery device and a recovery method for gaseous hydrocarbon, which can efficiently remove the gaseous hydrocarbon from the air flow containing the intermittently generated gaseous hydrocarbon and improve the working efficiency of the device. In the present invention, in a gaseous hydrocarbon recovery apparatus (100), a plurality of adsorption/desorption columns (14) are connected in parallel with respect to a gas-liquid separator (8) when adsorbing gaseous hydrocarbons, and two of the adsorption/desorption columns (14) for adsorbing gaseous hydrocarbons are connected in series via a gaseous hydrocarbon feed pump (5), a condensing device, and the gas-liquid separator (8) when desorbing gaseous hydrocarbons.
Description
Technical field
The present invention relates to the retracting device and the method for hydrocarbon gas contained in airborne release gas, particularly, the retracting device and the method thereof that relate to the hydrocarbon gas that is used for handling the high flammable gasoline vapour of the volatility such as gasoline that produce at fueling facilities such as gas stations.
Background technology
Removing in the method for the hydrocarbon gas in the past that has used condensing unit and adsorption-desorption device, following method is arranged, promptly, supply with the gas (exhaust gas that contains the gasoline vapour of the 40vol% that has an appointment) that produces from exhaust gas generation source to condensing unit by pump, hydrocarbon gas is cooled off, then, the exhaust gas of handling by the condensation operation that will be through with is to the adsorption-desorption unit feeding, hydrocarbon gas is removed in absorption, discharges in atmosphere as the cleaned air that contains the hydrocarbon gas below the 1vol% (clean air).Under the situation of this method, adsorption-desorption device one side is alternately switched above-mentioned absorption process and following desorption step, and one side is carried out running, still, decides this switching by the cumulant of the supply gas flow of hydrocarbon gas.
On the other hand, through the purge gas carrier pipe, adsorption-desorption device behind the absorption process that is through with is carried purge gas, to by attracting adsorbed hydrocarbon gas to carry out desorb with vavuum pump.As purge gas, the part of the gas of discharging from the top of adsorption-desorption device when using the absorption running makes the vavuum pump running with about 20～30kPa (Pascal).The air that contains the hydrocarbon gas after the desorb is transported to the upstream side of pump, with after the gas that produces from exhaust gas generation source mixes, to condensing unit and adsorption-desorption unit feeding.Condensing unit is cooled off indirectly by the heat medium that is frozen the machine cooling.In addition, in order to cool off the adsorbent layer in the adsorption-desorption device, this heat medium is also passed through the liquid pump to the adsorption-desorption unit feeding.
By such structure, hydrocarbon gas can be as roughly full dose liquid gasoline recovery.Therefore, in such method, the concentration of the hydrocarbon gas of discharging from the adsorption-desorption device is very low, can reach the level (for example, with reference to patent documentation 1) that can not cause atmosphere pollution.
[technical literature formerly]
[patent documentation]
[patent documentation 1] spy open the 2006-198604 communique (the 9th～16 page, Figure 10)
Summary of the invention
But,, reclaim in the method for hydrocarbon gas at the such use condensing unit and the adsorption-desorption device of patent documentation 1 record, if the gas flow of handling increases, then the pressure loss at condensing unit and adsorption-desorption device increases, and accompanies with it, also must increase pump capacity.In addition, the noise of generation also increases, and as the method under the big situation of the gas flow of handling, is not to be the method for reality.
In addition, if the gas flow of handling increases, then can not carry out smoothly by the hydrocarbon of condensing unit cooling, liquefaction and hydrocarbon gas separating at gas-liquid separator, also produce vaporific hydrocarbon to the adsorption-desorption unit feeding, caused the problem of the adsorption capacity reduction etc. of adsorbent easily.For fear of such situation, also considered increase adsorption-desorption device, use the situation of a large amount of adsorbents, still, the pressure loss of adsorption-desorption device increases, and must make pump capacity bigger.
Have again, under the situation of the recovery of the hydrocarbon gas that is used for spilling, be necessary the corresponding a large amount of hydrocarbon gas that produce of time band that refueling to the subsurface storage jar from the subsurface storage jar of fueling facility.Therefore, must with the peak value of the hydrocarbon gas that produces design apparatus ability correspondingly, produced and make device big to having surpassed necessary needs.Have, only in the time band work of refueling to the subsurface storage jar, the device work ratio is extremely bad again.
The present invention is the invention that produces in order to solve problem as described above, its objective is that providing a kind of can remove hydrocarbon gas efficiently from the air stream that contains hydrocarbon gas that produces off and on, improved the retracting device and the method for the hydrocarbon gas of device work ratio.
Relevant hydrocarbon gas retracting device of the present invention, it is characterized in that having: from the gasoline storage tank attract hydrocarbon gas pump, will cool off by the hydrocarbon gas that said pump attracts, the condensing unit of condensation, the gas-liquid separator that will separate with the hydrocarbon gas of failing by above-mentioned condensing unit condensation by the aqueous hydrocarbon of above-mentioned condensing unit condensation, to carry out a plurality of adsorption-desorption towers of adsorption-desorption from above-mentioned gas-liquid separator effluent air shape hydrocarbon; When carrying out the absorption of hydrocarbon gas, make from above-mentioned gas-liquid separator effluent air shape hydrocarbon and flow into above-mentioned a plurality of adsorption-desorption tower, when carrying out the desorb of hydrocarbon gas, at least one the adsorption-desorption tower in above-mentioned a plurality of adsorption-desorption towers connects in the mode of the upstream side that becomes said pump.
Relevant hydrocarbon gas recovery method of the present invention, it is characterized in that, comprise following operation, promptly, attract hydrocarbon gas from the gasoline storage tank, with the hydrocarbon gas cooling that attracts, condensation, with the intact hydrocarbon gas branch of condensation that fails, make it to flow into a plurality of adsorption-desorption towers, operation at separately adsorption-desorption tower adsorbed gas shape hydrocarbon, the operation that the attraction of above-mentioned gas shape hydrocarbon is stopped, an adsorbed hydrocarbon gas of adsorption-desorption tower to two adsorption-desorption towers of the absorption that is used for hydrocarbon gas attracts desorb, with first step for regeneration of hydrocarbon gas residual behind this hydrocarbon gas that liquefied with another adsorption-desorption tower absorption, above-mentioned another adsorption-desorption tower is connected in the mode that becomes upstream side, hydrocarbon gas to above-mentioned another adsorption-desorption tower absorption attracts desorb, with second step for regeneration of hydrocarbon gas residual behind this hydrocarbon gas that liquefied with above-mentioned adsorption-desorption tower absorption, the operation of above-mentioned first step for regeneration of stipulated number and above-mentioned second step for regeneration repeatedly.
The invention effect
According to relevant hydrocarbon gas retracting device of the present invention and method, even handling gas flow increases, also can make exhaust gas extremely clean (cleaning that gasoline concentration 1vol% is following) by a plurality of adsorption-desorption tower adsorbed gas shape hydrocarbons.
Description of drawings
Fig. 1 is the summary construction diagram of loop structure of the hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression.
Fig. 2 is the summary construction diagram of structure of first heat exchanger that carries on the hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression.
Fig. 3 is the skeleton diagram of internal structure of the gas-liquid separator that carries on the hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression.
Fig. 4 result's that to be expression investigation mist amount exert one's influence to the exit concentration of the hydrocarbon gas of the adsorption-desorption tower that carries on the hydrocarbon gas retracting device of relevant embodiments of the present invention 1 chart.
Fig. 5 is the loop diagram of the hydrocarbon gas stream in the step for regeneration of hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression.
Fig. 6 is the flow chart of the handling process in the step for regeneration of hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression.
Fig. 7 is the chart of the relation that changes the exit concentration of the exit concentration of exit concentration, gas-liquid separator of the hydrocarbon gas supply pump in the step for regeneration of hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression and adsorption-desorption tower and time.
Fig. 8 is the chart of relation of the exit concentration of switching time in the step for regeneration of hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression and adsorption-desorption tower.
Fig. 9 is the chart of the relation that changes the exit concentration of the exit concentration of the hydrocarbon gas supply pump in the step for regeneration of hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression and gas-liquid separator and time.
Figure 10 is the chart of the relation of the inlet pressure of the gas flow of hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression and hydrocarbon gas supply pump and outlet pressure.
Figure 11 is the chart of the relation of the gas flow of hydrocarbon gas retracting device of the relevant embodiments of the present invention 1 of expression and gas temperature.
Figure 12 is the summary construction diagram of loop structure of the hydrocarbon gas retracting device of the relevant embodiments of the present invention 2 of expression.
Figure 13 is the flow chart of the handling process in the step for regeneration of hydrocarbon gas retracting device of the relevant embodiments of the present invention 2 of expression.
Figure 14 is the flow chart of the handling process in the step for regeneration of hydrocarbon gas retracting device of the relevant embodiments of the present invention 3 of expression.
Figure 15 is the summary construction diagram that is used to illustrate first heat exchanger that carries of relevant embodiments of the present invention 4 on the hydrocarbon gas retracting device.
The specific embodiment
Below, with reference to the accompanying drawings, embodiments of the present invention are described.
Fig. 1 is the summary construction diagram of loop structure of the hydrocarbon gas retracting device 100 of the relevant embodiments of the present invention 1 of expression.According to Fig. 1, the loop structure and the hydrocarbon gas stream of the hydrocarbon gas retracting device 100 of relevant embodiment 1 is described.In addition, comprise Fig. 1, among the figure below, have the size relationship situation different of each component parts with the actual size relation interior.In addition, in Fig. 1, the hydrocarbon gas stream during the performed absorption process of expression hydrocarbon gas retracting device 100.
Hydrocarbon gas retracting device 100 is arranged on the gasoline fueling facility such as gas station, and the hydrocarbon gas that is discharged in atmosphere by set gasoline fueling facility is adsorbed (recovery), desorb (utilizing) again.This hydrocarbon gas retracting device 100 is used for reclaiming the hydrocarbon gas that repeatedly operation in a day produced (from the oil truck that transports gasoline etc. when gasoline storage tank 1 is supplied with gasoline, the hydrocarbon gas of extruding from gasoline storage tank 1) in order to handle.
This hydrocarbon gas retracting device 100 has gasoline storage tank 1, oil filling pipe 2, three-way switch valve 3 (three-way switch valve 3a, three-way switch valve 3b), pressure-regulating valve 4, hydrocarbon gas supply pump 5, first heat exchanger 6, heat medium accumulator tank 7, gas-liquid separator 8, aqueous hydrocarbon accumulator tank 9, aqueous hydrocarbon magnetic valve 10, liquid circulation pump 11, refrigerator 12, second heat exchanger 13, adsorption-desorption tower 14 (adsorption-desorption tower 14a, adsorption-desorption tower 14b), pressure controller 15, four groups of two-port valves (two-port valve 16a and two-port valve 17a as cross valve, two-port valve 16b and two-port valve 17b, two-port valve 18a and two-port valve 19a, two-port valve 18b and two-port valve 19b), flow controller 20, controller 50.
It is inferior that gasoline storage tank 1 is arranged on the ground of fueling facility, the gasoline that storage is supplied with from oil truck etc.Oil filling pipe 2 is using when gasoline storage tank 1 is supplied with gasoline from oil truck etc.Three-way switch valve 3 is connected with gasoline storage tank 1 through pipe arrangement, switches from the flow direction of the air that contains hydrocarbon gas of gasoline storage tank 1 attraction.Three-way switch valve 3a is respectively in the threeway one and is connected with gasoline storage tank 1, and in the threeway one is connected with three-way switch valve 3b, and in the threeway one is connected with the path that hydrocarbon gas is discharged to atmosphere.Three-way switch valve 3b is respectively in the threeway one and is connected with three-way switch valve 3a, and in the threeway one is connected with hydrocarbon gas supply pump 5, and in the threeway one is connected with adsorption-desorption tower 14.
Switch by three-way switch valve 3a, hydrocarbon gas is had pressure-regulating valve 4 on the path that atmosphere is discharged, pressure-regulating valve 4 is adjusted the pressure of the hydrocarbon gas of discharging to atmosphere.Hydrocarbon gas supply pump 5 will be attracted in device by the hydrocarbon gas that gasoline storage tank 1 produces.First heat exchanger 6 is arranged on the downstream of hydrocarbon gas supply pump 5, the hydrocarbon gas that cooling is attracted.This first heat exchanger 6 has the stream of a plurality of hydrocarbon gas.Heat medium accumulator tank 7 is accommodated first heat exchanger 6 in inside, store the heat medium (for example, water, salt water etc.) of this first heat exchanger 6 of cooling.
Gas-liquid separator 8 is arranged on the downstream of first heat exchanger 6, will be separated with residual hydrocarbon gas by the aqueous hydrocarbon of first heat exchanger, 6 cooling condensations.The aqueous hydrocarbon accumulator tank 9 interim aqueous hydrocarbons that separate by gas-liquid separator 8 that store.Aqueous hydrocarbon flows to the flow of the aqueous hydrocarbon of aqueous hydrocarbon accumulator tank 9 from gas-liquid separator 8 with magnetic valve 10 controls.Liquid circulation pump 11 is sent the heat medium that is stored by heat medium accumulator tank 7 from heat medium accumulator tank 7 to adsorption-desorption tower 14.The heat medium that refrigerator 12 is stored by heat medium accumulator tank 7 by 13 coolings of second heat exchanger.
Two-port valve 16a and two-port valve 17a are set between the gas-liquid separator 8 and adsorption-desorption tower 14 of hydrocarbon gas stream, by switching is controlled, make hydrocarbon gas and adsorption-desorption tower 14 conductings as adsorption tower performance function.In Fig. 1, with two-port valve 16a and two-port valve 17a blacking, but the state of expression conducting ground control hydrocarbon gas.Two-port valve 16b and two-port valve 17b are set at the part that three-way switch valve 3b is connected with adsorption-desorption tower 14, by switching is controlled, make the aqueous hydrocarbon and the three-way switch valve 3b conducting of desorb from adsorption-desorption tower 14 as desorber performance function.In Fig. 1, two-port valve 16b and two-port valve 17b are marked into hollow, the state that expression can not conducting ground control hydrocarbon gas.
Two-port valve 18a and two-port valve 19a are set on the drain passageway of the air that contains hydrocarbon gas that is connected with adsorption-desorption tower 14, by switching is controlled, with outwards gas discharge of gas (cleaned air).In Fig. 1, with two-port valve 18a and two-port valve 19a blacking, but the state of expression conducting ground control gas.Two-port valve 18b and two-port valve 19b are set at separating on the intake channel that smokes air of being connected with adsorption-desorption tower 14, by switching is controlled, will separate the adsorption-desorption tower 14 of suck importing as desorber performance function.In Fig. 1, two-port valve 18b and two-port valve 19b to be marked into hollow, expression can not conducting ground control desorb air state.The flow of separating suck that flow controller 20 controls are supplied with to adsorption-desorption tower 14.
The switching of control device 50 control two-port valves (two-port valve 16a, two-port valve 16b, two-port valve 17a, two-port valve 17b, two-port valve 18a, two-port valve 18b, two-port valve 19a, two-port valve 19b), the driving of the switching of the stream of three-way switch valve 3, the driving of hydrocarbon gas supply pump 5/stop, liquid circulation pump 11/stop, the adjustment of pressure controller 15, the aperture of flow controller 20 etc. have been passed through.This control device 50 for example can be made of micro computer etc.The handling process of the flow chart shown in addition, is carried out by control device 50 controls.
The running action of hydrocarbon gas retracting device 100 is described.
The running of hydrocarbon gas retracting device 100 is carried out with absorption (recovery) operation and these two steps of regeneration (desorb) operation usually.Therefore, behind the explanation absorption process, step for regeneration is described.Usually, in hydrocarbon gas retracting device 100, stream is switched to the airborne release side, be controlled to unlike the authorized pressure height by the pressure of pressure-regulating valve 4 with gasoline storage tank 1 by three-way switch valve 3a.In addition, in present embodiment 1, describe having as the action under the situation of two basic adsorption-desorption towers 14 of hydrocarbon gas retracting device 100.
[absorption process]
From oil truck etc. through oil filling pipe 2 when gasoline storage tank 1 is supplied with gasoline, three-way switch valve 3a is switched to retracting device side (three-way switch valve 3b side), simultaneously, three-way switch valve 3b is switched, and links to each other with hydrocarbon gas supply pump 5 with gasoline storage tank 1.At this moment, if beginning is supplied with gasoline to gasoline storage tank 1, the hydrocarbon gas that then riddles gasoline storage tank 1 is discharged from gasoline storage tank 1.The hydrocarbon concentration of the hydrocarbon gas of this moment is about 30～40vol% at normal temperatures.
The hydrocarbon gas of discharging from gasoline storage tank 1, is carried to first heat exchanger 6 by hydrocarbon gas supply pump 5 through three- way switch valve 3a and 3b with air.First heat exchanger 6 is by the heat medium cooling that is frozen machine 12 and 13 coolings of second heat exchanger.Usually, the inside of first heat exchanger 6 remains on about 0 ℃ to 5 ℃, contained condensate moisture in the part of hydrocarbon gas and the gas.Therefore, the air that contains hydrocarbon gas that flow into first heat exchanger 6 flows out from first heat exchanger 6 as the mixing object that has mixed aqueous hydrocarbon, hydrocarbon gas, water, air state.This mixes object and flows into gas-liquid separator 8.
The mixing object that flow into gas-liquid separator 8 is separated into gas (hydrocarbon gas and air) and liquid (aqueous hydrocarbon and water) by gas-liquid separator 8.Separated liquid retention is stored temporarily in aqueous hydrocarbon accumulator tank 9 through aqueous hydrocarbon with magnetic valve 10 at the downside of gas-liquid separator 8.In this hydrocarbon gas retracting device 100, as shown in Figure 1, hydrocarbon gas is gone into circulation from the upside of first heat exchanger 6.So, aqueous hydrocarbon and moisture flow downwards effectively because of gravity and gas stream, and the recovery of these liquefaction things is easy.
But, be that 0.5MPa (G), chilling temperature are to turn round under 5 ℃ the condition if make first heat exchanger 6 at pressure, be under the situation of gasoline vapour then at hydrocarbon gas, in first heat exchanger 6, gasoline vapour concentration is about 10vol%.Usually contain butane, iso-butane etc. in the gasoline vapour.It is that 0.5MPa (G), temperature are 5 ℃ of down their saturated concentrations during running at pressure that investigation makes first heat exchanger 6, and the result is that the saturated vapor concentration of butane is about 20vol%, and the saturated vapor concentration of iso-butane is about 30vol%.Under this condition, under the situation that the butane that contains in gasoline vapour, the amount of iso-butane do not have to reduce, gasoline vapour concentration can not reach below the 10vol% in theory.
In addition, by reducing temperature (at the chilling temperature of the gasoline vapour of first heat exchanger 6), can be reduced in the gasoline vapour concentration of the outlet of first heat exchanger 6.But below freezing, then contained water freezes at first heat exchanger 6 in the gas (air that contains hydrocarbon gas) as if the design temperature that makes first heat exchanger 6.So, increase in the loss of first heat exchanger, 6 pressure inside, therefore, the design temperature of wishing first heat exchanger 6 is about 0 ℃ to 5 ℃.
Then, the hydrocarbon gas of discharging from gas-liquid separator 8 is transported to the adsorption-desorption tower 14 that connects in parallel, is adsorbed processing.That is, as shown in Figure 1, two adsorption-desorption towers 14 all flow into the hydrocarbon gas of discharging from gas-liquid separator 8.Therefore, be in two-port valve 16a, two-port valve 17a, two-port valve 18a, two-port valve 19a open (blacking), two-port valve 16b, two-port valve 17b, two-port valve 18b, two-port valve 19b close (whitewashing), and flow controller 20 cuts out the state of (whitewashing).In addition, the gas of discharging from adsorption-desorption tower 14 is discharged into the atmosphere through pressure controller 15.
Enclose the adsorbent that above-mentioned such adsorbed gas shape hydrocarbon is arranged in the adsorption-desorption tower 14.In hydrocarbon gas retracting device 100,, mainly use silica gel as the adsorbent of hydrocarbon gas.Particularly, effectively have the silica gel in 4～10 independent dust apertures or synthetic zeolite or their mixture as adsorbent.That is, pass through in such adsorbent by making hydrocarbon gas, hydrocarbon gas is removed in absorption, becomes the clean air of the following gasoline concentration of 1vol%, through pressure controller 15 to airborne release.
Adsorption-desorption tower 14 is irrelevant with the effect of the adsorption-desorption of hydrocarbon gas, the temperature that the heat medium that quilt is supplied with by liquid circulation pump 11 is cooled to stipulate.That is, the always controlled running of the cooling system of first heat exchanger 6 is so that maintain as design temperature 0～5 ℃ by the refrigerator 12 and second heat exchanger 13.Its reason is, because the adsorbent that is filled in adsorption-desorption tower 14 is by the heat transfer cooling from the heat exchanger of fin-tube heat exchanger etc. (not shown go out), so cool time to a certain degree is integral, and running that can not corresponding moment.Have again, can produce harmful effect to equipment cost in the situation that the short time is cooled off the big refrigerator of such cooling capacity 12, cheap device can not be provided because have.
In addition,, can increase adsorption capacity, reduce the use amount of adsorbent by reducing adsorption-desorption tower 14 temperature inside.But, below freezing, then,, produce the problem of the gasoline adsorption capacity reduction of adsorbent in adsorption-desorption tower 14 so ice is put aside gradually at adsorbent because water freezes as if the internal temperature that makes adsorption-desorption tower 14.Therefore, wish that the internal temperature of adsorption-desorption tower 14 is above freezing.Based on above-mentioned situation, unified by the cooling system that makes first heat exchanger 6 and adsorption-desorption tower 14 in hydrocarbon gas retracting device 100, can reclaim hydrocarbon gas effectively.
For the internal pressure that makes adsorption-desorption tower 14 is pressure 0.5MPa (G) when the absorption, be about 0.02MPa when desorb, and adsorption-desorption tower 14 is made cylindrical conformation.By adsorption-desorption tower 14 is made cylindrical conformation, can make the pressure equalization that is applied to internal face.Therefore, even the pressure in the adsorption-desorption tower 14 are pressurized state, negative pressure state, can warpage etc. yet, can realize safe adsorption-desorption tower 14.In addition,, consider heat transfer, configuration fin-tube heat exchanger (by the aluminium fin time temperature media stream to heat-transfer pipe) to silica gel, synthetic zeolite equigranular adsorbent in the inside of adsorption-desorption tower 14.
Then,, between the aluminium fin, insert adsorbent, prevent nut, prevent that adsorbent from flowing out pipe arrangement, simultaneously, make gas flow good in the outflow of upper and lower settings adsorbent at adsorption-desorption tower 14.Under this situation, even in order to make hydrocarbon gas to the absorption of adsorbent, the cowling panel by making such as perforated metals also can be set, so that hydrocarbon gas flows equably at adsorption-desorption tower 14.Setting in the mode parallel with the flow direction of hydrocarbon gas towards hope of the fin of fin-tube heat exchanger is so that the pressure loss can not become hydrocarbon gas and flow the time.In addition, for cooling effectively is filled near the outer wall adsorbent, also can carry out between fin-tube heat exchanger and outer wall, can not producing the research in gap.
Under this situation, with regard to side with blow vent, be provided with and partly contact such clathrate, tabular metal (aluminium of heat-transfer character excellence, copper the best) with blow vent, with regard to the side that does not have blow vent, long by length than the fin of fin-tube heat exchanger itself, eliminate the gap between outer wall and the fin-tube heat exchanger, this situation is effective.In addition, in order to eliminate the gap portion between outer wall and the fin-tube heat exchanger, also can insert metal bar, finned pipe etc.Have again, wish that before entering heat-transfer pipe, the pipe arrangement branch with heat medium flows is divided into a plurality of with fin-tube heat exchanger, make heat medium in parallel mobile.So, can reduce the pressure loss of the mobile pipe arrangement of heat medium, can reduce the capacity of heat medium to the liquid circulation pump 11 of adsorption-desorption tower 14 supplies.
Have again, in adsorption-desorption tower 14, because hydrocarbon gas flows from bottom to top, so, wish to prevent that the mode that nut joins from disposing so that the granulated sorbent of fin-tube heat exchanger and bottom flows out.In view of the above, can prevent to eliminate the space between nut and the fin-tube heat exchanger, that is, only fill the space of granulated sorbent, can when absorption, fully implement the cooling of granulated sorbent in the granulated sorbent outflow.Its result is, can prevent that the temperature of the existing hydrocarbon gas of part that the hydrocarbon gas at maximum concentration enters from rising, and safe adsorption-desorption tower 14 can be provided.In addition, under the situation that hydrocarbon gas flows from the top down, can certainly make the granulated sorbent outflow on top prevent that nut and fin-tube heat exchanger from joining.
Under the situation that first heat exchanger 6 is not set, because the hydrocarbon gas of high concentration flows into adsorption-desorption tower 14, simultaneously, contained moisture is adsorbed agent absorption in the hydrocarbon gas, the absorption property of hydrocarbon gas reduces, so, the loading of adsorbent is increased.In addition, be reduced under the situation below freezing, existed generation moisture to freeze the possibility of the fault that gas obstruction etc. are big on the surface of adsorbent in temperature with adsorption-desorption tower 14.
Therefore, hydrocarbon gas retracting device 100 in relevant present embodiment 1 is provided with first heat exchanger and gas-liquid separator 8 because of the leading portion at adsorption-desorption tower 14, so, moisture is removed with hydrocarbon gas, can prevent the harmful effect of the moisture in the adsorption-desorption tower 14 in advance.In addition, can significantly reduce quantity delivered, simultaneously, can prevent that vaporific hydrocarbon from entering (describing in detail among Fig. 3), therefore, can dwindle adsorption-desorption tower 14, can make at an easy rate to adsorption-desorption tower 14 gas supplied shape hydrocarbons.
Have again, in the hydrocarbon gas retracting device 100 of relevant present embodiment 1, because the hydrocarbon gas of the high concentration (40vol%) of discharging from gasoline storage tank 1 is reduced to 10vol% by first heat exchanger 6, so the amount of gasoline of being handled by adsorption-desorption tower 14 is lowered to 1/4 (=10%/40%) with respect to whole traffic attractions.That is, be provided with first heat exchanger 6 and gas-liquid separator 8, can make the volume of adsorption-desorption tower 14 be roughly 1/4 by leading portion at adsorption-desorption tower 14.
[step for regeneration]
The step for regeneration of adsorption-desorption tower 14 is carried out in the following manner, promptly, two adsorption-desorption towers 14 that use during the absorption of hydrocarbon gas (two the adsorption-desorption towers 14 of adsorption-desorption tower that are used for the absorption of hydrocarbon gas) connect in the mode of series connection, connect hydrocarbon gas supply pump 5, first heat exchanger 6, gas-liquid separator 8 between this two tower.Promptly, using gases shape hydrocarbon supply pump 5, attract gas from an adsorption-desorption tower 14 (for example adsorption-desorption tower 14b), the hydrocarbon gas that is adsorbed agent absorption is carried out desorb, supply with to first heat exchanger 6, gas-liquid separator 8 successively, supply with the gas of discharging to another adsorption-desorption tower 14 (for example adsorption-desorption tower 14a), carry out the regeneration of hydrocarbon gas from gas-liquid separator 8.
Again in other words, hydrocarbon gas retracting device 100 is when adsorbed gas shape hydrocarbon (during absorption process), make from gas-liquid separator 8 effluent air shape hydrocarbons and flow into whole adsorption-desorption towers 14, when hydrocarbon gas is carried out desorb (during step for regeneration), at least one adsorption-desorption tower 14 in a plurality of adsorption-desorption towers 14 (for example adsorption-desorption tower 14b) is connected the upstream side of hydrocarbon gas supply pump 5.Just switch stream by two-port valve, so that when adsorbed gas shape hydrocarbon, make from gas-liquid separator 8 effluent air shape hydrocarbons and flow into whole adsorption-desorption towers 14, when hydrocarbon gas is carried out desorb, switch stream, so that the gas vent of at least one adsorption-desorption tower 14 in the adsorption-desorption tower 14 (for example adsorption-desorption tower 14b) is connected the upstream side of hydrocarbon gas supply pump 5.
After having continued the stipulated time running, switch the switching of two-port valve, never carry out adsorption-desorption tower (for example adsorption-desorption tower 14a) the adsorption-desorption hydrocarbon gas of desorb.Promptly, using gases shape hydrocarbon supply pump 5, attract gas from the opposing party's adsorption-desorption tower 14 (for example adsorption-desorption tower 14a), the hydrocarbon gas that is adsorbed agent absorption is carried out desorb, supply with to first heat exchanger 6, gas-liquid separator 8 successively, to supply with to an adsorption-desorption tower 14 (for example adsorption-desorption tower 14b) from the gas that gas-liquid separator 8 is discharged, carry out the regeneration of hydrocarbon gas.In the hydrocarbon gas retracting device 100 of relevant present embodiment 1, the regeneration of hydrocarbon gas is carried out in such operation of stipulated number repeatedly.
Fig. 2 is the summary construction diagram of the structure of expression first heat exchanger 6.According to Fig. 2, first heat exchanger 6, second heat exchanger 13, refrigerator 12 and the heat medium accumulator tank 7 of hydrocarbon gas retracting device 100 is described.First heat exchanger 6 has the stream that hydrocarbon gas flows.The cold-producing medium that 13 conductings of second heat exchanger are supplied with from refrigerator 12.Refrigerator 12 has freeze cycle, to second heat exchanger, 13 the supply system cryogens.Heat medium accumulator tank 7 stores the heat medium that first heat exchanger 6 is cooled off.Constitute condensing unit by first heat exchanger 6, second heat exchanger 13, refrigerator 12 and heat medium accumulator tank 7.
As shown in Figure 2, first heat exchanger 6 has the stream that a plurality of hydrocarbon gas flow.That is, the heat exchange department 22 that constitutes by the branching portion (collector) 21 that the hydrocarbon gas stream that flows into is cut apart, by the fin-tube heat exchanger that is inserted with at a plurality of heat-transfer pipes of branching portion 21 branches of first heat exchanger 6, the hydrocarbon gas that will discharge from heat exchange department 22 and the interflow portion (Off Star タ one) 23 at aqueous hydrocarbon interflow constitute.By first heat exchanger 6 is made such structure, can reduce the flow velocity of the air that contains hydrocarbon gas, can not can reduce heat exchanger effectiveness, and the pressure loss is reduced.
In addition, do not make the air branch of the hydrocarbon gas that contains big flow, under the situation about cooling off with first heat exchanger 6,, be necessary to make the contact area of heat exchange department 22 to increase in order to accelerate flow velocity.For contact area is increased, be necessary to make the piping length of heat-transfer pipe to increase.Therefore, because piping length increases, produced the problem that the pressure loss further increases.For to should problem, by at first heat exchanger 6, the stream that hydrocarbon gas is flowed branches into a plurality of, prevents the situation of pressure loss geometry character ground increase, can efficiently hydrocarbon gas be liquefied.
Then, the validity of having used the cooling that condensing unit brings is described.
Usually, under the situation of carrying out heat exchange, do not use heat medium etc., the refrigerant piping and object (hydrocarbon gas) pipe arrangement that is cooled is integrated, should integrated part to make thermal insulation construction the most effective.But, contain in cooling under the situation of air of moisture, can not freeze in order to make moisture, be necessary to make the evaporating temperature of cold-producing medium above freezing.Under this situation, produce heat exchanger effectiveness and reduce, the object that is cooled can not be cooled to the problem of set point of temperature.
In the hydrocarbon gas retracting device 100 of relevant present embodiment 1, it is characterized in that, use heat medium, by making heat medium free convection, can cool off effectively.Because in first heat exchanger 6, by the power of gravity and gas stream, aqueous hydrocarbon is discharged, so, hydrocarbon gas flows into from the top of first heat exchanger 6, and gas shape and aqueous hydrocarbon flow out from the bottom of first heat exchanger 6.Therefore, supply with hot hydrocarbon gas to the top of first heat exchanger 6, the temperature of the heat medium of the top periphery of first heat exchanger 6 rises.In view of the above, at the periphery of first heat exchanger 6, heat medium produces flowing from bottom to top.
On the other hand, at the periphery of second heat exchanger 13, because heat medium is cooled, so heat medium produces flowing from the top down.In view of the above, at heat medium accumulator tank 7, produce the such heat medium stream in the first heat exchanger top → second heat exchanger top → second heat exchanger bottom → first heat exchanger bottom, even do not stir etc., the object that is cooled (first heat exchanger 6) also can be cooled off effectively.Therefore, wish that first heat exchanger 6 and second heat exchanger 13 are arranged in the heat medium accumulator tank 7 in the mode that becomes the approximate horizontal position.
In addition, in hydrocarbon gas retracting device 100, because by liquid circulation pump 11, heat medium is supplied with to adsorption-desorption tower 14, so, synchronous by the stream that makes the free convection generation in the stream that produces because of the circulation of this heat medium and the heat medium accumulator tank 7, can more effectively cool off processed object.Promptly, as an example, extract heat medium out by bottom from second heat exchanger 13, make heat medium turn back to the top of second heat exchanger 13, can not hinder the such heat medium stream in the first heat exchanger top → second heat exchanger top → second heat exchanger bottom → first heat exchanger bottom, and can cool off processed object effectively.
Because above-mentioned situation, the hydrocarbon gas retracting device 100 of relevant present embodiment 1 constitutes condensing unit by first heat exchanger 6, second heat exchanger 13, refrigerator 12, heat medium accumulator tank 7, simultaneously, first heat exchanger 6 and second heat exchanger 13 are configured in heat medium accumulator tank 7, so that heat medium moves at above-below direction, in view of the above, produce convection current, can cool off the object that is cooled effectively in the inside of heat medium accumulator tank 7.
Fig. 3 is the skeleton diagram of the internal structure of expression gas-liquid separator 8.According to Fig. 3, the hydrocarbon that describes gas-liquid separator 8 in detail is removed the impact of performance.As shown in Figure 3, gas-liquid separator 8 has hydrocarbon gas outlet 24, centrifugation portion (gas-liquid separation portion) 25, gas-liquid mixture inlet 26, aqueous hydrocarbon storage portion 27, aqueous hydrocarbon outlet 28, taper screen cloth (mist is removed portion) 29 and heat-barrier material 30.That is, gas-liquid separator 8 has hydrocarbon gas and liquefaction hydrocarbon position (centrifugation portion 25) of separating and the position that hydrocarbon gas is separated with vaporific hydrocarbon (as the taper screen configuration, being taper screen cloth 29).
Gas-liquid mixture inlet 26 becomes the inflow entrance of hydrocarbon gas (comprising air) and aqueous hydrocarbon.Centrifugation portion 25 will be from gas-liquid mixture 26 hydrocarbon gas and the aqueous hydrocarbon centrifugations that flow into that enter the mouth.Hydrocarbon gas outlet 24 flow exports that become by centrifugation portion 25 gas separated.Aqueous hydrocarbon storage portion 27 stores the liquid that is separated by centrifugation portion 25.Aqueous hydrocarbon outlet 28 becomes the outlet of the liquid that is stored in aqueous hydrocarbon storage portion 27.Taper screen cloth 29 is removed vaporific hydrocarbon effectively.Heat-barrier material 30 reduces giving and accepting of heat between gas-liquid separators 8 inside and outside.
By 25 centrifugations of centrifugation portion, gas and liquid are separated from gas-liquid mixture inlet 26 hydrocarbon gas of coming in and aqueous hydrocarbon.But, because if handling flow increases, then aqueous hydrocarbon is accelerated to the impact velocity of the wall of centrifugation portion 25, so, from the vaporific hydrocarbon of aqueous nytron deposits yields.Because vaporific hydrocarbon is by 25 centrifugations of centrifugation portion, so, exist to adsorption-desorption tower 14 and supply with, the problem that makes the performance of the adsorbent of adsorption-desorption tower reduce soon.In order to prevent the generation of this problem, be necessary to remove vaporific hydrocarbon.In order to remove vaporific hydrocarbon, effectively possesses the screen cloth that the aperture is the degree that mist conflicted.
But, have under the situation of screen cloth, if screen cloth is blocked in mist and screen cloth collision, then the pressure loss increases, and therefore, is necessary to remove effectively the mist attached on the screen cloth.Therefore, the gas-liquid separator 8 at hydrocarbon gas retracting device 100 is provided with the taper screen cloth 29 that cross sectional shape is a upside-down triangle shape.The mist that collides taper screen cloth 29 moves to the central portion that does not have flowing gas substantially (the downside summit of upside-down triangle shape) because of gravity, and is a certain amount of as if having compiled, and then drips.Like this, taper screen cloth 29 is set, can removes the mist that produces because of wall collision effectively, can avoid the performance of adsorption-desorption tower 14 to reduce as far as possible with gas-liquid separator 8 by the top in centrifugation portion 25.
Fig. 4 is that the chart of mist amount to the result of the influence of the exit concentration of the hydrocarbon gas of adsorption-desorption tower 14 investigated in expression.According to Fig. 4, the influence of the amount of vaporific hydrocarbon to the exit concentration of the hydrocarbon gas of adsorption-desorption tower 14 is described.In this Fig. 4, investigated the mist amount to 500L/min, make hydrocarbon gas flow into the influence of exit concentration of the hydrocarbon gas of the adsorption-desorption tower 14 under 20 minutes the situation.In addition, in Fig. 4, be respectively the longitudinal axis represent from adsorption-desorption tower 14 spill concentration (vol%), transverse axis represents to flow into the mist amount of adsorption-desorption tower 14.
As shown in Figure 4, known following investigation result, promptly, in the mist amount that flows into adsorption-desorption tower 14 ((a) shown in Figure 4) under 0 the situation, the concentration that spills from adsorption-desorption tower 14 is 4vol%, in the mist amount that flows into adsorption-desorption tower 14 ((b) shown in Figure 4) under the situation of 100mL/min, the concentration that spills from adsorption-desorption tower 14 is 6vol%, being ((c) shown in Figure 4) under the situation of 200mL/min in the mist amount that flows into adsorption-desorption tower 14, is 8vol% from the concentration that spills of adsorption-desorption tower 14.
As can be seen from Figure 4, by preventing the inflow of mist, can suppress the concentration of the hydrocarbon gas that the adsorption-desorption tower 14 when having handled the hydrocarbon gas of ormal weight discharges to adsorption-desorption tower 14.Based on above-mentioned situation, possesses gas-liquid separator 8, this gas-liquid separator 8 has hydrocarbon gas and liquefaction hydrocarbon position of separating and the position that hydrocarbon gas is separated with vaporific hydrocarbon, in view of the above, can reduce to adsorption-desorption tower 14 gas supplied shape hydrocarbon amounts, can reclaim hydrocarbon gas efficiently.
The running start method of hydrocarbon gas retracting device 100 is described.
Hydrocarbon gas retracting device 100 also can by the driver's operation of oil truck etc. entry into service during step switch.That is, also can be with gasoline when the driver of the oil truck of gasoline storage tank 1 unloading (supply) etc. is unloading gasoline, entry into service when having operated the step switch of hydrocarbon gas retracting device 100.In view of the above, misoperation can be prevented, hydrocarbon gas can be reclaimed efficiently.
In addition, prevent that with regard to possessing oil truck from causing oil to plant with regard to the wrong retracting device that mixes anti-locking apparatus (not shown go out), the also key apparatus interlock that can differentiate with the oil kind in when beginning of unloading, hydrocarbon gas retracting device 100 beginnings running automatically.In view of the above, people's operation can be alleviated, hydrocarbon gas can be more stably reclaimed.Have again, the also oil gauge that can manage (not shown go out) interlock with quantity in stock (Fuel Oil Remaining) to gasoline storage tank 1, by the change of pasta position, detect the situation that quantity in stock changed in the short time, the 100 automatic entrys into service of hydrocarbon gas retracting device.Have again, also can link with this device, running is begun automatically and finish to the pouring orifice of gasoline storage tank 1 unloading the electronic sensor (catching the variation (not shown go out) of voltage etc.) of tracer liquid being set from oil truck.In view of the above, can not need people's operation, simultaneously, needn't newly possess senior metering device, can more stably reclaim hydrocarbon gas.
Fig. 5 is the loop diagram of the hydrocarbon gas stream in the step for regeneration of expression hydrocarbon gas retracting device 100.Fig. 6 is the flow chart of the handling process in the step for regeneration of expression hydrocarbon gas retracting device 100.According to Fig. 5 and Fig. 6, describe the step for regeneration of the hydrocarbon gas that is adsorbed desorber 14 absorption in detail, that is, and the desorption process of hydrocarbon gas.As mentioned above, two adsorption-desorption towers 14 that the step for regeneration of adsorption-desorption tower 14 used with when absorption be series connection, and the mode of connection hydrocarbon gas supply pump 5, first heat exchanger 6, gas-liquid separator 8 begins between this two tower.Then,, change the order of the adsorption-desorption tower 14 that is connected in series, all carry out the regeneration of hydrocarbon gas from adsorption-desorption tower 14 arbitrarily through after the stipulated time.Carry out this operation of stipulated number repeatedly, carry out the regeneration of hydrocarbon gas.
Hydrocarbon gas retracting device 100 makes all two-port valves when absorption finishes be full cut-off.Hydrocarbon gas retracting device 100 is opened (step S101) with two-port valve 16a, two-port valve 17b, two-port valve 18a, two-port valve 19b, makes 5 work (step S102) of hydrocarbon gas supply pump.Begin first operation (step S101～S105) like this.By making the 5 work stipulated times of hydrocarbon gas supply pump, through two-port valve 17b, attract gas from adsorption-desorption tower 14b, the hydrocarbon gas that is adsorbed agent absorption is carried out desorb (step S103).In addition,, then open two-port valve 19b and stream controller 20, make the air of certain flow flow into adsorption-desorption tower 14b, adsorption-desorption tower 14b pressure inside is roughly maintained necessarily from atmosphere if the pressure in the adsorption-desorption tower 14b is reduced to authorized pressure.
Though adsorption-desorption tower 14b pressure with 0.5MPa (G) when absorption moves, but when desorb, reduced pressure below the atmospheric pressure by hydrocarbon gas supply pump 5, therefore, the hydrocarbon that is adsorbed agent absorption by this pressure differential under the state of simmer down to high concentration by desorb.Under this situation, though depend on gas flow, the adsorbance when adsorbing of hydrocarbon gas, by the pressure in the adsorption-desorption tower 14b is controlled at 0.02～0.04MPa, can make hydrocarbon gas concentration is 30～60vol%.
Hydrocarbon gas after the desorb is supplied with to first heat exchanger 6 by hydrocarbon gas supply pump 5.That is be that 30vol%, pressure are the high concentration of 0.5MPa (G), the hydrocarbon gas of high pressure, to first heat exchanger, 6 supply gas shape hydrocarbon concentrations.Same during with absorption, first heat exchanger 6 is by the heat medium cooling by refrigerator 12 and 13 coolings of second heat exchanger.Usually, the inside of first heat exchanger 6 remains on about 0 ℃ to 5 ℃, a part of condensation liquefaction of hydrocarbon gas.
Therefore, supply with not at the hydrocarbon gas of first heat exchanger, 6 condensations and at the mixing object of the aqueous hydrocarbon of first heat exchanger, 6 condensations to gas-liquid separator 8.This mixing object is separated into gas (hydrocarbon gas and air) and liquid (aqueous hydrocarbon) (with reference to Fig. 3) by gas-liquid separator 8.Separated liquid retention turns back to aqueous hydrocarbon accumulator tank 9 through aqueous hydrocarbon with magnetic valve 10 the downside of gas-liquid separator 8 (aqueous hydrocarbon storage portion 27).
As mentioned above, be that 0.5MPa (G), chilling temperature are to turn round under 5 ℃ the condition if make first heat exchanger 6 at pressure, be under the situation of gasoline vapour then at hydrocarbon gas, in first heat exchanger 6, gasoline vapour concentration is about 10vol%.Usually contain butane, iso-butane etc. in the gasoline vapour.It is that 0.5MPa (G), temperature are their saturated concentration in 5 ℃ of whens running at pressure that investigation makes first heat exchanger 6, and the result is that the saturated vapor concentration of butane is about 20vol%, and the saturated vapor concentration of iso-butane is about 30vol%.Under this condition, under the situation that the butane that contains in gasoline vapour, the amount of iso-butane do not have to reduce, gasoline vapour concentration can not reach below the 10vol% in theory.
In addition, by reducing temperature (chilling temperature of the gasoline vapour of first heat exchanger 6), can reduce the gasoline vapour concentration of the outlet of first heat exchanger 6.But below freezing, then contained water freezes at second heat exchanger 6 in the gas (air that contains hydrocarbon gas) as if the design temperature that makes first heat exchanger 6.So, the loss of first heat exchanger, 6 pressure inside increases, and therefore, the design temperature of wishing first heat exchanger 6 is about 0 ℃ to 5 ℃.
Then, the hydrocarbon gas about the 10vol% that discharges from gas-liquid separator 8 is transported to adsorption-desorption tower 14a and handles.Enclose among the adsorption-desorption tower 14a adsorbent is arranged, the air that contains hydrocarbon gas passes through in this adsorbent, and in view of the above, hydrocarbon gas is adsorbed to be removed, become the clean air of the following gasoline concentration of 1vol%, through two-port valve 18a and pressure controller 15 to airborne release.Through after the stipulated time, stop hydrocarbon gas supply pump 5 (step S104), close two-port valve 16a, two-port valve 17b, two-port valve 18a, two-port valve 19b (step S105).In addition, also irrelevant even in when regeneration with the effect of the adsorption-desorption of hydrocarbon gas, always be cooled to uniform temperature by the heat medium of supplying with by liquid circulation pump 11.That is, equally always controlled running during with absorption is so that maintain 0～5 ℃.
Like this, in first operation (first step for regeneration),, can liquefy effectively and reclaim the hydrocarbon gas of discharging from adsorption-desorption tower 14b by cooling under pressurized state, absorption.In addition, when desorb, raise, desorption rate is accelerated, or hydrocarbon gas concentration is thickened by making adsorption-desorption tower 14b temperature inside.But, because temperature swing, the problem that exists consumed energy to increase or can not cool off in time etc. to next absorption process, therefore, aspect energy effectively, the temperature that when desorb, do not raise, but carry out desorb with temperature identical when adsorbing.
Hydrocarbon gas retracting device 100 then begins second operation (step S106～step S110) if be through with first operation.Hydrocarbon gas retracting device 100 is opened two-port valve 16b, two-port valve 17a, two-port valve 18b, two-port valve 19a (step S106), makes 5 work (step S107) of hydrocarbon gas supply pump.Like this, begin second operation (second step for regeneration).By making the 5 work stipulated times of hydrocarbon gas supply pump, attract gas through two-port valve 17b from adsorption-desorption tower 14a, the hydrocarbon gas that is adsorbed agent absorption is carried out desorb (step S108).In addition,, then open two-port valve 18b and flow controller 20, make the air of certain flow flow into adsorption-desorption tower 14a, maintain adsorption-desorption tower 14a pressure inside roughly certain from atmosphere if the pressure in the adsorption-desorption tower 14a is reduced to the pressure of regulation.
Though adsorption-desorption tower 14a pressure with 0.5MPa (G) when absorption moves, but when desorb, reduced pressure below the atmospheric pressure, therefore by hydrocarbon gas supply pump 5, by this pressure differential, the hydrocarbon that is adsorbed agent absorption under the state of simmer down to high concentration by desorb.Under this situation, though depend on gas flow, the adsorbance when adsorbing of hydrocarbon gas,, by the pressure in the adsorption-desorption tower 14a is controlled at 0.02～0.04MPa, can make hydrocarbon gas concentration is 30～60vol%.
Hydrocarbon gas after the desorb is supplied with to first heat exchanger 6 by hydrocarbon gas supply pump 5.That is be that 30vol%, pressure are the high concentration of 0.5MPa (G), the hydrocarbon gas of high pressure, to first heat exchanger, 6 supply gas shape hydrocarbon concentrations.Same during with absorption, first heat exchanger 6 is by the heat medium cooling by refrigerator 12 and 13 coolings of second heat exchanger.Usually, the inside of first heat exchanger 6 remains on about 0 ℃ to 5 ℃, a part of condensation liquefaction of hydrocarbon gas.
Therefore, supply with not at the hydrocarbon gas of first heat exchanger, 6 condensations and at the mixing object of the aqueous hydrocarbon of first heat exchanger, 6 condensations to gas-liquid separator 8.This mixing object is separated into gas (hydrocarbon gas and air) and liquid (aqueous hydrocarbon) (with reference to Fig. 3) by gas-liquid separator 8.Separated liquid retention turns back to aqueous hydrocarbon accumulator tank 9 through aqueous hydrocarbon with magnetic valve 10 the downside of gas-liquid separator 8 (aqueous hydrocarbon storage portion 27).
As mentioned above, be that 0.5MPa (G), chilling temperature are to turn round under 5 ℃ the condition if make first heat exchanger 6 at pressure, be under the situation of gasoline vapour then at hydrocarbon gas, in first heat exchanger 6, gasoline vapour concentration is about 10vol%.Usually contain butane, iso-butane etc. in the gasoline vapour.It is that 0.5MPa (G), temperature are their saturated concentration in 5 ℃ of whens running at pressure that investigation makes first heat exchanger 6, and the result is that the saturated vapor concentration of butane is about 20vol%, and the saturated vapor concentration of iso-butane is about 30vol%.Under this condition, under the situation that the butane that contains in gasoline vapour, the amount of iso-butane do not have to reduce, gasoline vapour concentration can not reach below the 10vol% in theory.
In addition, by reducing temperature (chilling temperature of the gasoline vapour of first heat exchanger 6), can reduce the gasoline vapour concentration of the outlet of first heat exchanger 6.But below freezing, then contained water freezes at second heat exchanger 6 in the gas (air that contains hydrocarbon gas) as if the design temperature that makes first heat exchanger 6.So, the loss of first heat exchanger, 6 pressure inside increases, and therefore, the design temperature of wishing first heat exchanger 6 is about 0 ℃ to 5 ℃.
Then, the hydrocarbon gas about the 10vol% that discharges from gas-liquid separator 8 is transported to adsorption-desorption tower 14b and handles.Enclose among the adsorption-desorption tower 14b adsorbent is arranged, the air that contains hydrocarbon gas passes through in this adsorbent, and in view of the above, hydrocarbon gas is adsorbed to be removed, become the clean air of the following gasoline concentration of 1vol%, through two-port valve 19a and pressure controller 15 to airborne release.Through after the stipulated time, stop hydrocarbon gas supply pump 5 (step S109), close two-port valve 16b, two-port valve 17a, two-port valve 18b, two-port valve 19a (step S110).In addition, even when regeneration is also irrelevant with the effect of the adsorption-desorption of hydrocarbon gas, always be cooled to uniform temperature by the heat medium of supplying with by liquid circulation pump 11.That is, equally always controlled running during with absorption is so that maintain 0～5 ℃.
If second operation finishes, then hydrocarbon gas retracting device 100 begins first operation (step S111) once more.After this operation of implementing set point number repeatedly, hydrocarbon gas retracting device 100 finishes a series of action (step S111; YES).Usually, refuel all these a series of operations repeatedly to gasoline storage tank 1 at every turn.By this action, only with the hydrocarbon gas of maximum 1vol% to airborne release, and can make carrying capacity of environment very little.
In addition, because hydrocarbon gas retracting device 100 is only with the discharging of the hydrocarbon gas of maximum 1vol%, so, can reclaim the 39vol% in the hydrocarbon gas of 40vol%, organic efficiency is 97.5%, efficient is very high.Have again, because be to have carried out carrying out behind the condensation operation adsorption operations at a temperature band, so, also have and can make significantly miniaturization of adsorption-desorption tower 14, can make the effect of device overall compactization.
Be arranged on the same section bottom of adsorption-desorption tower 14 (among the Fig. 1) of adsorption-desorption tower 14 when in addition, attracting during desorb to the position of adsorption-desorption tower 14 supply gas shape hydrocarbons from the position of the hydrocarbon gas of adsorption-desorption tower 14 and absorption.Because utilization adsorption-desorption tower 14, so that the hydrocarbon gas concentration that makes 14 outlets of adsorption-desorption tower is below 1vol%, so, become when absorption near the hydrocarbon gas steam suction inlet of adsorption-desorption tower 14, hydrocarbon gas adsorbs to high-density, near the hydrocarbon gas outlet of adsorption-desorption tower 14, the state how hydrocarbon gas does not adsorb.
For by condensation, from the hydrocarbon gas of adsorption-desorption tower 14 discharges, be necessary to improve as much as possible hydrocarbon gas concentration when reclaiming desorb effectively.That is, still discharge hydrocarbon gas, can discharge the hydrocarbon gas of high concentration from the part of absorption to high-density.Therefore, in hydrocarbon gas retracting device 100, by the part of adsorbing to high-density from hydrocarbon gas, promptly, near the hydrocarbon gas suction inlet when in adsorption-desorption tower 14, adsorbing, when desorb, attract to discharge hydrocarbon gas, can improve the organic efficiency of hydrocarbon gas.
Certain hour is regularly carried out in oiling to the gasoline storage tank 1 of fueling facilities such as gas station usually mostly.Therefore, produce hydrocarbon gas from gasoline storage tank 1 and be limited to certain regular hour band one day.Therefore, viewpoint from the operating efficiency that improves device, think effectively, be with the adsorption operations that carries out adsorption-desorption tower 14, carry out the regenerative operation of adsorption-desorption tower 14 at the time band that does not produce hydrocarbon gas in the time that produces hydrocarbon gas.
According to above-mentioned situation, the hydrocarbon gas retracting device 100 of relevant present embodiment 1 when absorption adsorption-desorption tower 14 to connect with respect to gas-liquid separator 8 modes parallel with one another, reduce the gas flow that flows to an adsorption-desorption tower 14, supply, connects the mode of two adsorption-desorption towers 14 with series connection when desorb from gas-liquid separator 8 effluent air shape hydrocarbons, carry out the adsorption-desorption operation repeatedly, carry out the regeneration of adsorbent, in view of the above, can realize the raising of operating efficiency.
Promptly, hydrocarbon gas retracting device 100 is (during absorption process) when the absorption of hydrocarbon gas, can make from gas-liquid separator 8 effluent air shape hydrocarbons and flow into whole adsorption-desorption towers 14, increase the flow of handling gas, when the desorb of hydrocarbon gas (during step for regeneration), at least one adsorption-desorption tower 14 in a plurality of adsorption-desorption towers 14 (for example adsorption-desorption tower 14b) is connected the upstream side of hydrocarbon gas supply pump 5, can carries out the regeneration of hydrocarbon gas.
Fig. 7 is the chart of the relation that changes the exit concentration of the exit concentration of exit concentration, gas-liquid separator 8 of the hydrocarbon gas supply pump 5 of expression in the step for regeneration and adsorption-desorption tower 14 and time.Fig. 8 is the switching time of expression in the step for regeneration and the chart of the relation of the exit concentration of adsorption-desorption tower 14.According to Fig. 7 and Fig. 8, the handover operation of the adsorption-desorption tower 14 in the step for regeneration is described.In Fig. 7, be respectively the longitudinal axis and represent the concentration of hydrocarbon gas (vol%), transverse axis is represented the time (min).In Fig. 8, be respectively the concentration (vol%) that the longitudinal axis is represented the hydrocarbon gas of adsorption-desorption tower 14 outlets, transverse axis is represented the time (min).
Be respectively the exit concentration of representing the hydrocarbon gas supply pump 5 in the step for regeneration of adsorption-desorption tower 14b with the open circles mark among Fig. 7, the exit concentration of representing the hydrocarbon gas supply pump 5 in the step for regeneration of adsorption-desorption tower 14b with the circle mark of blacking, the exit concentration of representing the gas-liquid separator 8 in the step for regeneration of adsorption-desorption tower 14b with hollow warning triangle, the exit concentration of representing the gas-liquid separator 8 in the step for regeneration of adsorption-desorption tower 14b with the warning triangle of blacking is represented the exit concentration of adsorption-desorption tower 14 with the asterisk mark.From this Fig. 7 as can be known, in step for regeneration, only hydrocarbon gas spills from adsorption-desorption tower 14 in the early stage.Therefore, investigate the influence of switching time to the exit concentration of adsorption-desorption tower 14.
Fig. 8 investigates first switching time to the figure of the influence of adsorption-desorption tower 14 exit concentrations.Among Fig. 8, be respectively the concentration of hydrocarbon gas of the outlet of the adsorption-desorption tower 14 when having represented to carry out the switching of one minute first operation first and second operation with diamond indicia, the concentration of the hydrocarbon gas of the outlet of the adsorption-desorption tower 14 when having represented to carry out the switching of three minutes first operation first and second operation with the fork mark, the concentration of the hydrocarbon gas of the outlet of the adsorption-desorption tower 14 when having represented to carry out the switching of six minutes first operation first and second operation with hollow warning triangle.As can be seen from Figure 8, along with the growth of switching time, the time of discharging hydrocarbon gas from 14 outlets of adsorption-desorption tower also increases.
In view of the situation, known first short more good more to the time that second operation is switched from first operation.On this basis, also clear, if make first from first operation to switching time of second operation below 0.5 minute, then at twice, hydrocarbon gas also spills from the adsorption tower outlet.From this result as can be known, by make first be 0.5 minute～1 minute from first operation to the switching time of second operation, can make the spilling of hydrocarbon gas in the step for regeneration be Min..
Fig. 9 is the chart of the relation that changes the exit concentration of the exit concentration of the hydrocarbon gas supply pump 5 of expression in the step for regeneration and gas-liquid separator 8 and time.According to Fig. 9, the influence of the switching time of the adsorption-desorption tower 14 in the step for regeneration to the recovery of hydrocarbon gas is described.In Fig. 9, be respectively the longitudinal axis and represent the concentration of hydrocarbon gas (vol%), transverse axis is represented the time (min).In addition, be respectively Fig. 9 (a) expression with the characteristic under the situation of interval switching in two fens, Fig. 9 (b) expression to be prolonging the characteristic under situation switching time in 2 minutes → 6 minutes → 10 minutes gradually, and Fig. 9 (c) expression is with the characteristic under 2 minutes → 1 minute → situation that shortened switching time gradually in 0.5 minute.In addition, circle mark and warning triangle shown in Figure 9 are identical with circle mark and warning triangle shown in Figure 7.
From shown in Fig. 9 (b) as can be known, by prolonging switching time gradually, the exit concentration of hydrocarbon gas supply pump 5 reduces.This is illustrated in the not liquefaction of first heat exchanger, 6 hydrocarbon gas.That is, the hydrocarbon gas of discharging from adsorption-desorption tower 14b only is that former state ground moves to adsorption-desorption tower 14a, and energy is consumed in vain.On the other hand, from shown in Fig. 9 (c) as can be known, by shortening switching time gradually, the reduction of the exit concentration of hydrocarbon gas supply pump 5 is inhibited.Hence one can see that, and the amount of the difference of the exit concentration of the exit concentration of hydrocarbon gas supply pump 5 and gas-liquid separator 8 is liquefied, and by switching, can effectively hydrocarbon gas be liquefied.
From above-mentioned situation as can be known, by accelerating (shortening) switching time that makes adsorption-desorption tower 14 gradually, can effectively hydrocarbon gas be liquefied.Therefore, in the hydrocarbon gas retracting device 100 of relevant present embodiment 1,, seek the raising of energy efficiency by accelerating gradually the switching time of adsorption-desorption tower 14.
Figure 10 is the chart of the relation of the inlet pressure of expression gas flow and hydrocarbon gas supply pump 5 and outlet pressure.Figure 11 is the chart of the relation of expression gas flow and gas temperature.According to Figure 10 and Figure 11, illustrate that gas flow is to the inlet pressure of hydrocarbon gas supply pump 5 and the influence of outlet pressure.Among Figure 10 and Figure 11, the influence of the gas flow when only using gases shape hydrocarbon supply pump 5 carries out the adsorption-desorption operation is described.
In Figure 10, be respectively the outlet pressure (kPa[abs]) that the left side longitudinal axis is represented hydrocarbon gas supply pump 5, the right side longitudinal axis is represented the inlet pressure (kPa[abs]) of hydrocarbon gas supply pump 5, transverse axis is represented gas flow (L/min).In addition, in Figure 10, be respectively the outlet pressure that warning triangle is represented hydrocarbon gas supply pump 5, circle mark is represented the inlet pressure of hydrocarbon gas supply pump 5.In Figure 11, be respectively the left side longitudinal axis represent gas temperature (℃), the right side longitudinal axis is represented compression ratio (-), transverse axis is represented gas flow (L/min).In addition, in Figure 11, be respectively warning triangle and represent gas temperature, circle mark is represented compression ratio.
From as can be known shown in Figure 10, along with gas flow increases, outlet pressure reduces, and in addition, along with gas flow increases, inlet pressure increases.In step for regeneration, because be necessary to improve hydrocarbon gas concentration, so, be necessary to reduce the pressure in the adsorption-desorption tower 14b.That is, be about 40vol% for making hydrocarbon gas concentration, must make inlet pressure below 40kPa.Therefore, gas flow is below 200L/min.In addition, under the situation that contains the butane that is difficult to liquefy, iso-butane, be necessary to make hydrocarbon gas concentration about 60vol%, must make inlet pressure below 30kPa.Therefore, gas flow is below 100L/min.
From as can be known shown in Figure 11, because if gas flow reduces, then the heat of being taken away by gas reduces, so gas temperature rises.Being under the situation of object with the gasoline vapour as hydrocarbon gas, because the natural ignition temperature of gasoline vapour is about 250 ℃, so, be necessary to make gas temperature to drop to below 200 ℃.That is,, must make gas flow more than 40L/min in order to make gas temperature below 200 ℃.From these situations as can be known, for using gases shape hydrocarbon supply pump 5 only carries out the adsorption-desorption operation, can make the scope of gas flow at 40～200L/min, good is the scope of 40～100L/min.
Based on above-mentioned situation, in the hydrocarbon gas retracting device 100 of relevant present embodiment 1, only use a hydrocarbon gas supply pump 5 to carry out the adsorption-desorption operation, flow by making the gas that flows to hydrocarbon gas supply pump 5 is in the scope of 40～200L/min, good is the scope of 40～100L/min, the recovery hydrocarbon gas that allows to liquefy effectively becomes possibility, realizes the raising of operating efficiency.
In the hydrocarbon gas retracting device 100 of relevant present embodiment 1,, carry out the regeneration of adsorption-desorption tower 14 by the gas displacement of carrying out at the shared attraction of step for regeneration and purge gas.But, implement in the short time to reduce the supply of purge gas as far as possible under the situation of switching of adsorption-desorption tower 14 to adsorption-desorption tower 14, also can stop the importing of purge gas.So,, can liquefy efficiently at first heat exchanger 6 because of the thin situation of purge gas with regard to the hydrocarbon gas concentration that do not have adsorption-desorption tower 14 outlet, recovery hydrocarbon gas more efficiently can liquefy.
As mentioned above, hydrocarbon gas retracting device 100 according to relevant present embodiment 1, by a plurality of adsorption-desorption towers 14 are connected in parallel when adsorbing, when desorb, be connected in series, can only carry out adsorption-desorptions with a hydrocarbon gas supply pump 5.Therefore, because can carry out absorption process by enough a plurality of adsorption-desorption towers 14, so, increase even handle gas flow, also can make exhaust gas extremely clean (gasoline concentration 1vol% is following).In addition, increase even handle gas flow, also can enough a plurality of adsorption-desorption tower 14 adsorbed gas shape hydrocarbons, can suppress to flow to the speed of the gas of adsorption-desorption tower 14, can reclaim hydrocarbon gas efficiently.
According to this hydrocarbon gas retracting device 100, because possess the condensing unit that constitutes by first heat exchanger 6, second heat exchanger 13 and heat medium accumulator tank 7, so, can not reduce the liquefaction efficiency of hydrocarbon gas, can not produce noise.In addition, hydrocarbon gas retracting device 100 has been because carried out research with keen determination to the structure of the gas-liquid separator 8 that carried, so, adsorption-desorption tower 14 employed adsorbents are increased, efficiently liquid gas shape hydrocarbons.
According to this hydrocarbon gas retracting device 100, because carry out first step for regeneration and second step for regeneration of stipulated number repeatedly, reclaim hydrocarbon gas, so, the hydrocarbon emission of adsorption-desorption tower 14 absorption can not arrived outside, can liquefy, can reclaim hydrocarbon gas efficiently.In addition, the capacity of the desorb correlation machine (hydrocarbon gas supply pump 5) of adsorption-desorption tower 14 can be reduced to be attached to, simultaneously, hydrocarbon gas can be reclaimed efficiently.
Figure 12 is the summary construction diagram of loop structure of the hydrocarbon gas retracting device 100a of the relevant embodiments of the present invention 2 of expression.According to Figure 12, the structure of hydrocarbon gas retracting device 100a and the flow process of hydrocarbon gas are described.This hydrocarbon gas retracting device 100a is also same with the hydrocarbon gas retracting device 100 of relevant embodiment 1, to the hydrocarbon gas that in atmosphere, discharges by set gasoline fueling facility adsorb, desorb.In addition, in embodiment 2, be that the center describes, to the part mark identical symbol identical with embodiment 1 with difference with embodiment 1.
About the hydrocarbon gas retracting device 100a of present embodiment 2 compares with the hydrocarbon gas retracting device 100 of relevant embodiment 1, difference is, possess hydrocarbon gas densimeter measuring device 31a in the downstream of hydrocarbon gas supply pump 5, possess hydrocarbon gas densimeter measuring device 31b in the downstream of gas-liquid separator 8.Hydrocarbon gas densimeter measuring device 31a and hydrocarbon gas densimeter measuring device 31b metering are in the concentration of the hydrocarbon gas of set pipe arrangement conducting.In addition, other structure of hydrocarbon gas retracting device 100a is identical with hydrocarbon gas retracting device 100.
Figure 13 is the flow chart of the handling process in the step for regeneration of expression hydrocarbon gas retracting device 100a.According to Figure 13, describe the step for regeneration of the hydrocarbon gas of adsorption-desorption tower 14 absorption in detail.As implement mode 1 illustrated, two the adsorption-desorption towers 14 that use when the step for regeneration of adsorption-desorption tower 14 makes absorption are series connection, connect hydrocarbon gas supply pump 5, first heat exchanger 6, gas-liquid separator 8, beginning between two tower.Like this,, change the order of the adsorption-desorption tower 14 that is connected in series, all carry out the regeneration of hydrocarbon gas from adsorption-desorption tower 14 arbitrarily through after the stipulated time.Carry out this operation of stipulated number repeatedly, carry out the regeneration of hydrocarbon gas.
Hydrocarbon gas retracting device 100a makes all two-port valves when absorption finishes be full cut-off.Hydrocarbon gas retracting device 100a opens (step S201) with two-port valve 16a, two-port valve 17b, two-port valve 18a, two-port valve 19b, makes 5 work (step S202) of hydrocarbon gas supply pump, beginning step for regeneration (first operation).Then, hydrocarbon gas retracting device 100a carries out concentration conditions evaluation (step S203) according to the concentration signal by hydrocarbon gas densimeter measuring device 31a and hydrocarbon gas densimeter measuring device 31b metering.Promptly, hydrocarbon gas retracting device 100a will be transmitted to control device 50 by the concentration signal of hydrocarbon gas densimeter measuring device 31a and hydrocarbon gas densimeter measuring device 31b metering, reached the situation of normal concentration, carried out the switching of adsorption-desorption tower 14.
If reach concentration (the step S203 of the regulation of the switching that is set to adsorption-desorption tower 14; YES), then hydrocarbon gas retracting device 100a stops hydrocarbon gas supply pump 5 (step S204), closes two-port valve 16a, two-port valve 17b, two-port valve 18a, two-port valve 19b (step S205).
Hydrocarbon gas retracting device 100a then begins second operation (step S106～step S110) if be through with first operation (step S201～step S205).Hydrocarbon gas retracting device 100 is opened two-port valve 16b, two-port valve 17a, two-port valve 18b, two-port valve 19a (step S206), makes 5 work (step S207) of hydrocarbon gas supply pump.Then, hydrocarbon gas retracting device 100a carries out concentration conditions evaluation (step S208) according to the concentration signal by hydrocarbon gas densimeter measuring device 31a and hydrocarbon gas densimeter measuring device 31b metering.
If reach concentration (the step S208 of the regulation of the switching that is set to adsorption-desorption tower 14; YES), then hydrocarbon gas retracting device 100a stops hydrocarbon gas supply pump 5 (step S209), closes two-port valve 16b, two-port valve 17a, two-port valve 18b, two-port valve 19a (step S210).If second operation finishes, then hydrocarbon gas retracting device 100a begins first operation (step S211) once more.After this operation of implementing set point number repeatedly, hydrocarbon gas retracting device 100a finishes a series of action (step S211; YES).
Like this, because hydrocarbon gas retracting device 100a carries out the switching of adsorption-desorption tower 14 according to the hydrocarbon gas concentration of metering, so, the switching of adsorption-desorption tower 14 can be carried out effectively, the energy of employed necessity of liquefaction of hydrocarbon gas can be reduced.Therefore, hydrocarbon gas retracting device 100a is on the basis of the effect of embodiment 1, even be stored at the quantitative changeization of the hydrocarbon gas of adsorption-desorption tower 14, recovery hydrocarbon gas efficiently also can liquefy.
Embodiment 3.
Figure 14 is the flow chart of the handling process in the step for regeneration of hydrocarbon gas retracting device of the relevant embodiments of the present invention 3 of expression.According to Figure 14, describe the step for regeneration of the adsorbed hydrocarbon gas of the adsorption-desorption tower 14 of hydrocarbon gas retracting device of relevant present embodiment 3 in detail.About the hydrocarbon gas retracting device of embodiment 3 also same with the hydrocarbon gas retracting device 100 of relevant embodiment 1, to the hydrocarbon gas that in atmosphere, discharges by set gasoline fueling facility adsorb, desorb.In addition, in embodiment 3, be that the center describes, to the part mark identical symbol identical with embodiment 1 and embodiment 2 with difference with embodiment 1 and embodiment 2.
In the hydrocarbon gas retracting device 100 of relevant above-mentioned embodiment 1, if moved the stipulated time at step for regeneration, then adsorption-desorption tower 14 is switched, if carried out this stipulated number repeatedly, and then desorb release, step for regeneration finishes.Relative therewith, the hydrocarbon gas retracting device of relevant present embodiment 3 (below the omission diagram, being called hydrocarbon gas retracting device 100b describes) in, if the perseveration that adsorption-desorption tower 14 is switched has carried out stipulated number, then reduce gas flow,, also reduce gas flow if the perseveration of the switching of adsorption-desorption tower 14 has carried out stipulated number, move such regeneration operating, gas flow is reduced to setting gradually.
That is, step S301～step S311 that hydrocarbon gas retracting device 100b carries out is identical with step S101～step S111 that the hydrocarbon gas retracting device of relevant embodiment 1 100 is carried out, but is appending difference on this aspect of step S312.In step S312, hydrocarbon gas retracting device 100b carries out the action that gas flow is reduced after the repeatable operation of first operation of having implemented set point number and second operation.(step S312 after gas flow is reduced to setting; YES), hydrocarbon gas retracting device 100b finishes a series of action.In addition, (step S312 when gas flow is not reduced to setting; NO), carry out first operation (step S301) once more.
In view of the above, hydrocarbon gas retracting device 100b is on the basis of the effect of embodiment 1 and embodiment 2, even be stored at the quantitative changeization of the hydrocarbon gas of adsorption-desorption tower 14, recovery hydrocarbon gas efficiently also can liquefy.In addition, because hydrocarbon gas retracting device 100b can reduce the number of occurrence of first operation and second operation, so having can be in the effect of chien shih hydrocarbon gas regeneration in short-term.
Figure 15 is the summary construction diagram that is used to illustrate first heat exchanger 32 that carries on the hydrocarbon gas retracting device of relevant embodiments of the present invention 4.According to Figure 15, describe first heat exchanger 32 in detail as the feature item of embodiment 4.About the hydrocarbon gas retracting device of embodiment 4 also same with the hydrocarbon gas retracting device 100 of relevant embodiment 1, to the hydrocarbon gas that in atmosphere, discharges by set gasoline fueling facility adsorb, desorb.In addition, in embodiment 4, be that the center describes, to the part mark identical symbol identical with embodiment 1～embodiment 3 with difference with embodiment 1～embodiment 3.
About the structure of first heat exchanger 32 of the hydrocarbon gas retracting device of present embodiment 4 different with the hydrocarbon gas retracting device of relevant above-mentioned embodiment.Though the basic structure of first heat exchanger 32 is identical with first heat exchanger 6,, the stream between heat exchange department 22 and interflow portion 23 (each isocon 35 (each heat-transfer pipe)) is provided with gas-liquid separator (second gas-liquid separator) 33.By first heat exchanger 32 is made such structure, can hydrocarbon gas be separated with aqueous hydrocarbon with low discharge, can improve separative efficiency.
In addition, in interflow portion 23, hydrocarbon gas and aqueous hydrocarbon mix, and can suppress the situation that the pressure loss increases, and can use the hydrocarbon gas supply pump 5 of low capacity, can seek the further raising of energy efficiency.Based on above-mentioned situation, the hydrocarbon gas retracting device of relevant embodiment 4 is on the basis of the effect of embodiment 1～embodiment 3, by on each of the isocon 35 of first heat exchanger 32, gas-liquid separator 33 being set, also has the effect that can improve energy efficiency.
In addition,, relevant hydrocarbon gas retracting device of the present invention and method be illustrated though being divided into embodiment 1～embodiment 4,, the feature item of each embodiment can certainly be made up rightly.
Symbol description
1: the gasoline storage tank; 2: oil filling pipe; 3: three-way switch valve; 3a: three-way switch valve; 3b: three-way switch valve; 4: pressure-regulating valve; 5: hydrocarbon gas supply pump (pump); 6: the first heat exchangers; 7: the heat medium accumulator tank; 8: gas-liquid separator; 9: aqueous hydrocarbon accumulator tank; 10: aqueous hydrocarbon magnetic valve; 11: liquid circulation pump; 12: refrigerator; 13: the second heat exchangers; 14: the adsorption-desorption tower; 14a: adsorption-desorption tower; 14b: adsorption-desorption tower; 15: pressure controller; 16a: two-port valve; 16b: two-port valve; 17a: two-port valve; 17b: two-port valve; 18a: two-port valve; 18b: two-port valve; 19a: two-port valve; 19b: two-port valve; 20: flow controller; 21: branching portion; 22: heat exchange department; 23: interflow section; 24: the hydrocarbon gas outlet; 25: centrifugation section; 26: the gas-liquid mixture entrance; 27: aqueous hydrocarbon storage unit; 28: aqueous hydrocarbon outlet; 29: the taper screen cloth; 30: heat-barrier material; 31a: hydrocarbon gas densimeter measuring device; 31b: hydrocarbon gas densimeter measuring device; 32: the first heat exchangers; 33: gas-liquid separator; 35: isocon; 100: the hydrocarbon gas retracting device; 100a: hydrocarbon gas retracting device.
Claims (15)
1. hydrocarbon gas retracting device is characterized in that having:
From the gasoline storage tank attract hydrocarbon gas pump,
The hydrocarbon gas cooling that will attract by said pump, the condensing unit of condensation,
The gas-liquid separator that will separate with the hydrocarbon gas of failing by above-mentioned condensing unit condensation by the aqueous hydrocarbon of above-mentioned condensing unit condensation,
To carry out a plurality of adsorption-desorption towers of adsorption-desorption from above-mentioned gas-liquid separator effluent air shape hydrocarbon;
When carrying out the absorption of hydrocarbon gas,
Make from above-mentioned gas-liquid separator effluent air shape hydrocarbon and flow into above-mentioned a plurality of adsorption-desorption tower,
When carrying out the desorb of hydrocarbon gas,
At least one adsorption-desorption tower in above-mentioned a plurality of adsorption-desorption tower connects in the mode of the upstream side that becomes said pump.
2. hydrocarbon gas retracting device as claimed in claim 1 is characterized in that,
Possess the cross valve that the gas vent from the stream of above-mentioned gas-liquid separator effluent air shape hydrocarbon and above-mentioned a plurality of adsorption-desorption towers is switched,
By above-mentioned cross valve,
When carrying out the absorption of hydrocarbon gas,
Switch stream, flow into above-mentioned a plurality of adsorption-desorption tower so that make from above-mentioned gas-liquid separator effluent air shape hydrocarbon,
When carrying out the desorb of hydrocarbon gas,
Switch stream, so that the gas vent of at least one the adsorption-desorption tower in above-mentioned a plurality of adsorption-desorption towers is connected to the upstream side of said pump.
3. hydrocarbon gas retracting device as claimed in claim 1 or 2 is characterized in that,
Above-mentioned condensing unit has at least:
First heat exchanger that can the conducting hydrocarbon gas,
Second heat exchanger of the cold-producing medium of can conducting supplying with from refrigerator,
The heat medium accumulator tank of the heat medium of heat exchange is carried out in storage by above-mentioned first heat exchanger and above-mentioned second heat exchanger.
4. hydrocarbon gas retracting device as claimed in claim 1 or 2 is characterized in that,
Above-mentioned first heat exchanger and above-mentioned second heat exchanger are set in the above-mentioned heat medium accumulator tank in the mode that becomes the approximate horizontal position,
The hydrocarbon gas of above-mentioned first heat exchanger inlet is arranged on top, the refrigerant inlet of above-mentioned second heat exchanger is arranged on the bottom.
5. hydrocarbon gas retracting device as claimed in claim 1 or 2 is characterized in that,
Above-mentioned first heat exchanger has:
The branching portion that the hydrocarbon gas stream that flows into is cut apart,
Be inserted with heat exchange department at a plurality of heat-transfer pipes of above-mentioned branching portion branch,
The hydrocarbon gas of discharging from above-mentioned heat exchange department and the interflow portion at aqueous hydrocarbon interflow,
Be arranged on second gas-liquid separator on the stream between above-mentioned heat exchange department and the above-mentioned interflow portion.
6. hydrocarbon gas retracting device as claimed in claim 1 or 2 is characterized in that,
Above-mentioned gas-liquid separator has:
The gas-liquid separation portion that hydrocarbon gas is separated with aqueous hydrocarbon,
The mist that will separate with hydrocarbon gas at the vaporific hydrocarbon that above-mentioned gas-liquid separation portion produces is removed portion.
7. hydrocarbon gas retracting device as claimed in claim 1 or 2 is characterized in that,
The above-mentioned mist portion of removing is the taper screen configuration.
8. a hydrocarbon gas recovery method is characterized in that, comprising:
Attract hydrocarbon gas, with hydrocarbon gas cooling, the condensation that attracts, the hydrocarbon gas branch that the condensation of failing is intact makes it to flow into a plurality of adsorption-desorption towers, the operation of separately adsorption-desorption tower adsorbed gas shape hydrocarbon,
The operation that the attraction of above-mentioned gas shape hydrocarbon is stopped,
An adsorbed hydrocarbon gas of adsorption-desorption tower to two adsorption-desorption towers of the absorption that is used for hydrocarbon gas attracts desorb, with hydrocarbon gas residual behind this hydrocarbon gas that liquefied with first step for regeneration of another adsorption-desorption tower absorption,
Above-mentioned another adsorption-desorption tower is connected in the mode that becomes upstream side, hydrocarbon gas to above-mentioned another adsorption-desorption tower absorption attracts desorb, second step for regeneration that hydrocarbon gas residual behind this hydrocarbon gas that liquefied is adsorbed with an above-mentioned adsorption-desorption tower,
The operation of above-mentioned first step for regeneration of stipulated number and above-mentioned second step for regeneration repeatedly.
9. hydrocarbon gas recovery method as claimed in claim 8 is characterized in that,
The time set that will switch to above-mentioned second step for regeneration from above-mentioned first step for regeneration first becomes shorter to the time that above-mentioned second step for regeneration switches than above-mentioned first step for regeneration hereafter.
10. hydrocarbon gas recovery method as claimed in claim 9 is characterized in that,
To it be 0.5～2 minute to the time set that above-mentioned second step for regeneration switches from above-mentioned above-mentioned first step for regeneration first.
11. as claim 9 or 10 described hydrocarbon gas recovery methods, it is characterized in that,
The mode that shortens to be accompanied by effluxion is set the reciprocal time of above-mentioned first step for regeneration and above-mentioned second step for regeneration.
12. as claim 9 or 10 described hydrocarbon gas recovery methods, it is characterized in that,
In above-mentioned first step for regeneration and above-mentioned second step for regeneration, the gas flow of hydrocarbon gas is set at 40～100L/min.
13. as claim 9 or 10 described hydrocarbon gas recovery methods, it is characterized in that, be provided with:
Attract hydrocarbon gas pump and
The gas-liquid separator that hydrocarbon gas is separated with aqueous hydrocarbon,
According to the hydrocarbon gas concentration of said pump outlet and the outlet of above-mentioned gas-liquid separator, above-mentioned first step for regeneration of stipulated number and above-mentioned second step for regeneration repeatedly.
14. as claim 9 or 10 described hydrocarbon gas recovery methods, it is characterized in that,
In said pump outlet and the outlet of above-mentioned gas-liquid separator the hydrocarbon gas measurement of concetration device of the concentration of measurement gas shape hydrocarbon is set, in the concentration of said pump outlet and above-mentioned gas-liquid separator outlet measurement gas shape hydrocarbon.
15. as claim 9 or 10 described hydrocarbon gas recovery methods, it is characterized in that,
After the operation of above-mentioned first step for regeneration of stipulated number and above-mentioned second step for regeneration finishes repeatedly,
Reduce the gas flow attracted, once more above-mentioned first step for regeneration of stipulated number and above-mentioned second step for regeneration repeatedly.
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| JP2009145490A JP5044764B2 (en) | 2009-06-18 | 2009-06-18 | Gaseous hydrocarbon recovery apparatus and method |
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- 2009-10-20 TW TW098135364A patent/TWI413544B/en not_active IP Right Cessation
- 2009-11-03 KR KR1020090105296A patent/KR101103228B1/en active IP Right Grant
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4462811A (en) * | 1983-07-26 | 1984-07-31 | John Zink Company | Process and apparatus for removing hydrocarbons from air-hydrocarbon vapor mixtures |
| CN1764709A (en) * | 2003-04-17 | 2006-04-26 | 三菱电机株式会社 | Gasification gasoline reclaiming device and reclaiming method |
| CN1807555A (en) * | 2004-12-22 | 2006-07-26 | 三菱电机株式会社 | Apparatus and method for treating and recovering gaseous hydrocarbons |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103100233A (en) * | 2011-11-10 | 2013-05-15 | 浙江大江山泵阀制造有限公司 | Comprehensive treatment method for organic solvent recovery and tail gas absorption during bulk drug drying process, and treatment system for achieving the same |
Also Published As
| Publication number | Publication date |
|---|---|
| TW201100159A (en) | 2011-01-01 |
| KR101103228B1 (en) | 2012-01-05 |
| TWI413544B (en) | 2013-11-01 |
| KR20100136392A (en) | 2010-12-28 |
| JP5044764B2 (en) | 2012-10-10 |
| JP2011000538A (en) | 2011-01-06 |
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Address after: Tokyo, Japan Applicant after: Missubishi Electric Co., Ltd. Applicant after: Tatsuno Corp. Address before: Tokyo, Japan Applicant before: Missubishi Electric Co., Ltd. Applicant before: Tatsuno Corp. |
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Application publication date: 20101229 |