CN101970082B - Device and method for treating and recovering gaseous hydrocarbon - Google Patents
Device and method for treating and recovering gaseous hydrocarbon Download PDFInfo
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- CN101970082B CN101970082B CN200880128078.4A CN200880128078A CN101970082B CN 101970082 B CN101970082 B CN 101970082B CN 200880128078 A CN200880128078 A CN 200880128078A CN 101970082 B CN101970082 B CN 101970082B
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- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 59
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 59
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 46
- 239000003502 gasoline Substances 0.000 claims abstract description 311
- 238000002336 sorption--desorption measurement Methods 0.000 claims abstract description 252
- 239000007788 liquid Substances 0.000 claims abstract description 98
- 238000001816 cooling Methods 0.000 claims abstract description 88
- 238000012545 processing Methods 0.000 claims abstract description 57
- 238000011084 recovery Methods 0.000 claims abstract description 14
- 238000001179 sorption measurement Methods 0.000 claims description 32
- 239000000110 cooling liquid Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 230000001276 controlling effect Effects 0.000 claims 2
- 230000001105 regulatory effect Effects 0.000 claims 1
- 238000009833 condensation Methods 0.000 abstract description 27
- 230000005494 condensation Effects 0.000 abstract description 27
- 239000007789 gas Substances 0.000 description 73
- 238000010521 absorption reaction Methods 0.000 description 37
- 238000010926 purge Methods 0.000 description 27
- 239000003463 adsorbent Substances 0.000 description 24
- 230000008569 process Effects 0.000 description 24
- 230000009471 action Effects 0.000 description 18
- 230000015572 biosynthetic process Effects 0.000 description 12
- 239000003208 petroleum Substances 0.000 description 12
- 238000007710 freezing Methods 0.000 description 10
- 230000008014 freezing Effects 0.000 description 10
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 9
- 239000000446 fuel Substances 0.000 description 8
- 239000013528 metallic particle Substances 0.000 description 8
- 239000000779 smoke Substances 0.000 description 7
- 238000013461 design Methods 0.000 description 6
- 238000007599 discharging Methods 0.000 description 6
- 238000003795 desorption Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 239000001273 butane Substances 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 239000000741 silica gel Substances 0.000 description 3
- 229910002027 silica gel Inorganic materials 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- -1 carbon hydrogen compound Chemical class 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000000280 densification Methods 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
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- 239000002826 coolant Substances 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- BGOFCVIGEYGEOF-UJPOAAIJSA-N helicin Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@H]1OC1=CC=CC=C1C=O BGOFCVIGEYGEOF-UJPOAAIJSA-N 0.000 description 1
- 230000008676 import Effects 0.000 description 1
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- 238000003825 pressing Methods 0.000 description 1
- ULWHHBHJGPPBCO-UHFFFAOYSA-N propane-1,1-diol Chemical class CCC(O)O ULWHHBHJGPPBCO-UHFFFAOYSA-N 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000001052 transient effect Effects 0.000 description 1
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Classifications
-
- 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
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
- B01D5/0006—Coils or serpentines
-
- 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
-
- 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
-
- 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
- B01D53/0438—Cooling or heating systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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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)
- Treating Waste Gases (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention provides a small-sized and cheap gaseous hydrocarbon processing and recovering device and method capable of effectively liquefying gasoline contained in gasoline vapor. A gasoline vapor recovery device (100) is characterized by comprising: a condenser pipe (3) for liquefying gasoline vapor; a gas-liquid separator (9) provided on the downstream side of the gas in the latter stage of the condensation pipe (3) and separating the gasoline liquid liquefied by the condensation pipe (3) from the gasoline vapor; an adsorption/desorption column (7) and an adsorption/desorption column (8)) which is provided on the downstream side of the gas in the latter stage of the gas-liquid separator (9) and which adsorbs/desorbs the gasoline vapor separated by the gas-liquid separator (9); a heat medium storage tank (4) for storing the heat medium, which stores the heat medium, and supplies the heat medium to the condenser pipe cooling tank (20) and the adsorption/desorption column, while storing and cooling the heat medium in the condenser pipe (3) and the adsorption/desorption column; and a refrigerator (6) for cooling the heat medium stored in the heat medium storage tank (4).
Description
Technical field
The present invention relates to processing retracting device and the method for vaporous hydrocarbon contained in the gas discharged to atmosphere, particularly relate to the device and method for the treatment of the gasoline vapor that when supplying with gasoline, spills.
Background technology
Remove in the method for vaporous hydrocarbon in the agent of existing use adsorption-desorption, from discharging gas (the discharge gas that contains the gasoline vapor of the 40vol% that has an appointment) that gas generation source produces with air blast or pressing certainly by discharging the gas snorkel and deliver to condenser, after in condenser, making a part of gasoline vapor liquefaction, the air that contains the gasoline vapor that does not have liquefaction is delivered to adsorption tower, the discharge gas of handling of finishing absorption process is discharged into the atmosphere as the air that contains the gasoline vapor below the 1vol% (clean air) by means of the top of discharge pipe from adsorption tower (adsorption tower after desorption step is switched).
In addition, in the adsorption tower after finishing absorption process, carry purge gas by means of the purge gas pipe, by carrying out desorb by the attraction of vavuum pump.As purge gas, use a part of clean air of when the absorption operation, discharging from the top of adsorption tower, so that becoming the mode of 100～300Torr, the adsorption tower internal pressure moves vavuum pump.
The purifying exhaust gas that contains gasoline vapor after the desorb with from discharging after the air that contains gasoline vapor that gas generation source produces mixes, deliver to condenser, in condenser, a part is liquefied, as the gasoline vapor in liquid (gasoline liquid) the reclaiming clean exhaust.
By such formation, can with gasoline vapor substantially all amounts reclaim as liquid gasoline, the concentration of the gasoline vapor of discharging from adsorption tower is fully low, can reach the level that does not cause atmosphere pollution.(for example with reference to patent documentation 1).
Patent documentation 1: TOHKEMY 2006-198604 communique (4-8 page or leaf, Fig. 2 and 9-16 page or leaf, Figure 10)
In addition, gasoline liquefaction amount in second condensing unit that the back segment of first condensing unit arranges seldom, the energy that consumes with the expense that second condensing unit is set or at second condensing unit comparatively speaking, the amount of gasoline of recovery is few, room for improvement is still being arranged aspect the efficient that reclaims at gasoline.
And then, in first condensing unit, because being arranged, airborne moisture sneaks into, so when chilling temperature being set at when below freezing, moisture freezes in first condensing unit causes first condensing unit to stop up, so, must be set in the chilling temperature of first condensing unit above freezing.But for such design temperature, as not liquefaction such as the butane of gasoline vapor principal component or pentane, keeping intact flow in the adsorption tower, thereby the time that spills gasoline vapor from adsorption tower shortens, and has the problem that shortens switching time of adsorption tower.Otherwise, for shorten the switching time that does not make adsorption tower, just must make adsorption tower become big, namely increase the amount that is filled into the adsorbent in the adsorption tower, thereby have the problem that causes device to maximize.
Summary of the invention
The present invention makes in order to solve above-mentioned problem, its objective is processing retracting device and method that the small-sized and cheap vaporous hydrocarbon that can effectively gasoline contained in the gasoline vapor be liquefied is provided.
The processing retracting device of vaporous hydrocarbon of the present invention, the processing retracting device of this vaporous hydrocarbon are used for gasoline vapor is handled, reclaimed, and it is characterized in that possessing: condensing unit, and this condensing unit liquefies gasoline vapor; Gas-liquid separator, this gas-liquid separator will be separated with gasoline vapor by the gasoline liquid of described condensing unit liquefaction; The adsorption-desorption device, this adsorption-desorption device carries out adsorption-desorption to the gasoline vapor by described gas-liquid separator separates; The thermal medium accumulator tank, this thermal medium accumulator tank stores the thermal medium of the described condensing unit of cooling and described adsorption-desorption device; The thermal medium that liquid circulation pump, this liquid circulation pump will be stored in the described thermal medium accumulator tank is supplied to described condensing unit and described adsorption-desorption device; Refrigerator, this refrigerator cooling is stored in the thermal medium in the described thermal medium accumulator tank; Valve, this valve adjustment is supplied to the thermal medium amount of described condensing unit; And control device, the temperature at the position that this control device mixes mutually according to the thermal medium and the thermal medium by described liquid circulation pump supply that are stored in the described condensing unit is controlled the switching of described valve.
The processing recovery method of vaporous hydrocarbon of the present invention, in the processing recovery method of this vaporous hydrocarbon, the attraction gasoline vapor also pressurizes, by condensing unit with this gasoline vapor cooling liquid, to be separated with gasoline vapor by the gasoline liquid of described condensing unit liquefaction, by the adsorption-desorption device gasoline vapor that separates is carried out adsorption-desorption, the thermal medium that is used for the cooling gasoline vapor to described condensing unit and described adsorption-desorption unit feeding, utilize refrigerator to cool off described thermal medium, it is characterized in that, by liquid circulation pump always to the thermal medium of described adsorption-desorption unit feeding cooling, the temperature at the position of mixing mutually according to the thermal medium and the thermal medium by described liquid circulation pump supply that are stored in the described condensing unit simultaneously, so that the gas temperature of the outlet of described condensing unit becomes the mode of set point of temperature, supply with the thermal medium of cooling to described condensing unit.
The processing recovery method of vaporous hydrocarbon of the present invention, in the processing recovery method of this vaporous hydrocarbon, the attraction gasoline vapor also pressurizes, by condensing unit with this gasoline vapor cooling liquid, to be separated with gasoline vapor by the gasoline liquid of described condensing unit liquefaction, by the adsorption-desorption device gasoline vapor that separates is carried out adsorption-desorption, the thermal medium that is used for the cooling gasoline vapor to described condensing unit and described adsorption-desorption unit feeding, utilize refrigerator to cool off described thermal medium, it is characterized in that, always to the thermal medium of described adsorption-desorption unit feeding cooling, simultaneously, so that the pressure differential of the gasoline vapor at place, the gateway of described condensing unit becomes the mode of authorized pressure, supply with the thermal medium of cooling to described condensing unit.
Processing retracting device according to vaporous hydrocarbon of the present invention, because the adsorption-desorption unit feeding thermal medium that can remove gasoline vapor to condensing unit and the absorption of liquified petroleum steam is respectively removed efficient so can improve the absorption of the gasoline vapor of adsorption-desorption device.Namely, in condensing unit, cause the pipe arrangement in the condensing unit to stop up because preventing airborne moisture freezes, simultaneously can make the temperature of adsorption tower lower than the temperature of condensing unit, remove gasoline vapor so can be adsorbed expeditiously by the adsorption-desorption device, realize the processing retracting device of reliability height, vaporous hydrocarbon that efficient is high.
According to the processing recovery method of vaporous hydrocarbon of the present invention, because the air that contains gasoline vapor that flows in condensing unit is cooled to set point of temperature above freezing, so the moisture in the gas does not freeze liquified petroleum steam effectively.
Description of drawings
Fig. 1 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 1.
Fig. 2 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 2.
Fig. 3 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 3.
Fig. 4 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 4.
Fig. 5 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 5.
Fig. 6 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 6.
Fig. 7 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 7.
Fig. 8 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 8.
Fig. 9 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 9.
Figure 10 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiment 10.
Description of reference numerals
1 fueller; 2 gasoline vapor suction pumps; 3 condenser pipes; 4 thermal medium accumulator tanks; 5 heat exchangers; 6 refrigerators; 7 adsorption-desorption towers; 8 adsorption-desorption towers; 9 gas-liquid separators; 10 liquid circulation pumps; 11 suction pumps; 12 gasoline grooves; 13 pressure controllers; 14 gasoline vapor carrier pipes; 15 discharge pipes that purify air; 16 Purge gas flow into pipe; 17 Purge gas discharge pipes; 18 gas-liquid mixed gasoline effusers; 19 temperature measuring devices; 20 condenser pipe cooling baths; 21 difference gauges; 31 second thermal medium cooling baths; 41 thermoregulators; 51 condensing containers; 52 condensation heat exchangers; 53 metallic particles; 61 second pressure controllers; 71 flow totalizers; 100 gasoline vapor retracting devices; 200 gasoline vapor retracting devices; 300 gasoline vapor retracting devices; 400 gasoline vapor retracting devices; 500 gasoline vapor retracting devices; 600 gasoline vapor retracting devices; 700 gasoline vapor retracting devices; 800 gasoline vapor retracting devices; 900 gasoline vapor retracting devices; 1000 gasoline vapor retracting devices; The B1 valve; The B2 valve; The B3 solution smokes valve; B3 ' solution smokes valve; B4 absorption dump valve; B4 ' absorption dump valve; The B5 mass flow controller; B5 ' mass flow controller; B6 absorption is with flowing into valve; B6 ' absorption is with flowing into valve; The B7 thermal medium is supplied with control valve; B8 thermal medium loopback valve; B9 second thermal medium is supplied with control valve; B10 the 3rd thermal medium is supplied with control valve; The C1 triple valve; The C2 triple valve; The C3 triple valve; The C4 triple valve; The C5 triple valve.
The specific embodiment
Below, based on accompanying drawing embodiments of the present invention are described.
Fig. 1 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 1.Based on Fig. 1 formation and the action of the processing retracting device (the following gasoline vapor retracting device 100 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 100 is when supplying with gasoline contained gasoline in discharged to the gasoline vapor in the atmosphere to be liquefied and reclaim.In addition, comprise Fig. 1, the relation situation different with actual state of the size of each component parts arranged in following accompanying drawing.In addition, two-wire is represented the conducting of thermal medium, and common solid line or dotted line represent to contain the conducting of the air of gasoline vapor, and heavy line is represented the conducting of gasoline liquid.
As shown in Figure 1, gasoline vapor retracting device 100 has: fueller 1, gasoline vapor suction pump 2, condenser pipe 3, thermal medium accumulator tank 4, heat exchanger 5, refrigerator 6, adsorption-desorption tower (adsorption-desorption tower 7 and adsorption-desorption tower 8), gas-liquid separator 9, liquid circulation pump 10, suction pump 11, gasoline groove 12, pressure controller 13, gasoline vapor carrier pipe 14, the discharge pipe 15 that purifies air, Purge gas flow into pipe 16, Purge gas discharge pipe 17, gas-liquid mixed gasoline effuser 18, temperature measuring device 19 and condenser pipe cooling bath 20.In addition, in gasoline vapor retracting device 100, valve B1, valve B2, solution are set smoke valve B3, absorption and supply with control valve B7 and triple valve (triple valve C1～C4) with dump valve B4, mass flow controller B5, absorption with flowing into valve B6, thermal medium.
Below, the function of each component part of gasoline vapor retracting device 100 is described.Fueller 1 has fuel feeding nozzle etc., has function from gasoline to the motor vehicle of passenger car or motorcycle etc. that supply with.The function of the entrance when in addition, fueller 1 performance sucks the gasoline vapor that spills when supplying with gasoline.Gasoline vapor suction pump 2 is connected with the upstream side of fueller 1 with condenser pipe 3, has the function that near the gasoline vapor that will produce the fuel feeding portion of fueller 1 is drawn into gasoline vapor retracting device 100 inside.
Thermal medium accumulator tank 4 is connected with liquid circulation pump 10 with condenser pipe cooling bath 20, store heat medium (being the non freezing solution that material etc. constitutes by the oil that is called propane diols or gasoline, kerosene for example).Heat exchanger 5 is located in the thermal medium accumulator tank 4, has the function that cooling is stored in the thermal medium in the thermal medium accumulator tank 4 as a component part of refrigerator 6.Refrigerator 6 is connected with thermal medium accumulator tank 4 by means of heat exchanger 5, simultaneously with gasoline vapor suction pump 2 and suction pump 11 between Purge gas discharge pipe 17 be connected, have the function of heat exchanger 5 the supply system cryogens by utilizing heat pump cycle.In addition, the connection status of refrigerator 6 and heat exchanger 5 is represented with chain-dotted line.
Adsorption-desorption tower 7 and adsorption-desorption tower 8 form that circulation has the thermal medium that is stored in the thermal medium accumulator tank 4 and the mode of the air that contains gasoline vapor that flows out from condenser pipe 3, have the function as the adsorption-desorption device of absorption, desorb gasoline vapor.In this adsorption-desorption tower 7 and adsorption-desorption tower 8, be filled with absorption or remove the adsorbent (for example silica gel or zeolite etc.) that (desorb) contains the airborne gasoline vapor of gasoline vapor.In addition, in Fig. 1, be that example represent as adsorption tower, adsorption-desorption tower 8 as the situation of desorber work with adsorption-desorption tower 7.Gas-liquid separator 9 is connected with adsorption-desorption tower 7 and adsorption-desorption tower 8 with the downstream of condenser pipe 3, has separation by the gasoline liquid of condenser pipe 3 liquefaction and the function of gasoline vapor.In addition, gasoline liquid is directed into gasoline groove 12, and gasoline vapor is directed into adsorption-desorption tower 7 or adsorption-desorption tower 8.
Gasoline vapor carrier pipe 14 is connected with gas-liquid separator 9, and on the way branch is connected with adsorption-desorption tower 7 and adsorption-desorption tower 8 simultaneously, the air guide adsorption-desorption tower 7 or the adsorption-desorption tower 8 that contain gasoline vapor from gas-liquid separator 9.The discharge pipe 15 that purifies air is connected with pressure controller 13, and the air (clean air that contains the gasoline vapor below the 1vol%) from adsorption- desorption tower 7 and 8 discharges of adsorption-desorption tower is sent to atmosphere.Purge gas flows into pipe 16 and is connected with the discharge pipe 15 that purifies air, be connected with adsorption-desorption tower 8 with adsorption-desorption tower 7 simultaneously, from adsorption-desorption tower 7 or adsorption-desorption tower 8 delivers to adsorption-desorption tower 8 discharged to a part of clean gas of atmosphere as Purge gas or adsorption-desorption tower 7 uses.
Purge gas discharge pipe 17 is connected with suction pump 11, and on the way branch is connected with adsorption-desorption tower 7 and adsorption-desorption tower 8 simultaneously, the Purge gas after conducting is utilized by adsorption- desorption tower 7 or 8 desorbs of adsorption-desorption tower.Gas-liquid mixed gasoline effuser 18 is connected with gas-liquid separator 9 with the downstream of condenser pipe 3, and conducting is by the gasoline liquid of condenser pipe 3 liquefaction and contain the air of gasoline vapor.Temperature measuring device 19 is arranged near the downstream of condenser pipe 3, the temperature of the air that contains gasoline vapor of be determined at condenser pipe 3 conductings, discharging from condenser pipe 3.Temperature information by this temperature measuring device 19 is measured is transported to diagram abridged control device as signal.
Valve B1 is connected with fueller 1, simultaneously with gasoline vapor suction pump 2 and refrigerator 6 between Purge gas discharge pipe 17 be connected, open linkedly with the work of fueller 1.Valve B2 is connected with gasoline groove 12 with gas-liquid separator 9, opens when the gasoline liquid that is reclaimed by gas-liquid separator 9 is supplied to gasoline groove 12.Solution smokes the Purge gas discharge pipe 17 that valve B3 is located at each branch respectively, opens when the conducting Purge gas by open and close controlling.In addition, below, smoke valve B3 and call solution and smoke valve B3 ' and describe being located at solution on the Purge gas discharge pipe 17 that is connected with adsorption-desorption tower 7.
Absorption is located on adsorption-desorption tower 7 and adsorption-desorption tower 8 and each pipe arrangement that pressure controller 13 is connected with dump valve B4, comes the air that contains gasoline vapor after conducting is adsorbed by adsorption-desorption tower 7 and adsorption-desorption tower 8 by open and close controlling.In addition, below, be located on the pipe arrangement that is connected with adsorption-desorption tower 8 absorption with dump valve B4 call absorption use dump valve B4 ' to describe.Each Purge gas that mass flow controller B5 is located at across the discharge pipe 15 that purifies air flows into pipe 16, controls the gas flow of Purge gas by open and close controlling.In addition, below, the mass flow controller B5 that is located at the Purge gas inflow pipe 16 that is connected with adsorption-desorption tower 7 is called mass flow controller B5 ' describe.
Absorption is located on each gasoline vapor carrier pipe 14 of branch with flowing into valve B6, comes the air that contains gasoline vapor is imported adsorption-desorption tower 7 or adsorption-desorption tower 8 by open and close controlling.In addition, below, the absorption of being located in the gasoline vapor carrier pipe 14 that is connected with adsorption-desorption tower 8 is called absorption and describes with inflow valve B6 ' with flowing into valve B6.Thermal medium is supplied with control valve B7 and is located between liquid circulation pump 10 and the condenser pipe cooling bath 20, adjusts the amount that is supplied to the thermal medium of condenser pipe cooling bath 20 from thermal medium accumulator tank 4 by open and close controlling.
Triple valve C1 is connected with condenser pipe cooling bath 20, thermal medium accumulator tank 4 and triple valve C2, changes the circulation destination of thermal medium by switching controls.Triple valve C2 is connected with adsorption-desorption tower 7, adsorption-desorption tower 8 and triple valve C1, changes the circulation destination of thermal medium by switching controls.Triple valve C3 is connected with condenser pipe cooling bath 20, liquid circulation pump 10 and triple valve C4, changes the circulation destination of thermal medium by switching controls.Triple valve C4 is connected with adsorption-desorption tower 7, adsorption-desorption tower 8 and triple valve C3, changes the circulation destination of thermal medium by switching controls.The control of the switching of the stream of the switching of each valve or each triple valve in addition,, refrigerator 6 etc. are carried out by diagram abridged control device.
Then, the action to gasoline vapor retracting device 100 describes.When fueller 1 work, linkedly valve B1 is opened 2 actions of gasoline vapor suction pump with it.When gasoline vapor suction pump 2 began to move, near the gasoline vapor (about 40vol% at normal temperatures) the fuel feeding portion of fueller 1 was drawn in the gasoline vapor retracting device 100, for example was compressed to about 0.2～0.4MPa and delivered to condenser pipe 3.Condenser pipe 3 is located in the condenser pipe cooling bath 20, by the thermal medium cooling that is stored in the condenser pipe cooling bath 20.Usually, condenser pipe cooling bath 20 inside remain on about 0 ℃ to 5 ℃, and in condenser pipe 3 during conducting, contained some condensation of moisture in gasoline and the gas is separated into gas (gasoline vapor) and liquid (gasoline) by means of gas-liquid separator 9 at gasoline vapor.
In addition, in the service condition of condenser pipe 3, be that pressure is that 0.3MPa, chilling temperature are that 5 ℃, gas flow are under the condition of 100L/min, the concentration of gasoline vapor is about 10vol%.In addition, from the saturated concentration line chart of gasoline vapor as can be known, be 0.3MPa at pressure, when temperature is 5 ℃, the saturated vapor oil vapor concentration is about 10vol%, and under this condition, gasoline vapor concentration can not become below the 10vol% in theory.In addition, descend by making temperature, can be reduced in the gasoline vapor concentration in the exit of condenser pipe 3.But, when design temperature when being below freezing, because contained water freezes at condenser pipe 3 in the gas, produce the pipe arrangement blocking problem of condenser pipe 3, so the design temperature of condenser pipe 3 is desirable about being set at from 0 ℃ to 5 ℃.
In addition, when supply time reached certain time, valve B2 opened.Thus, the gasoline liquid that remains in the bottom of gas-liquid separator 9 turns back to fueller 1 via gasoline groove 12.Thereafter, behind the process certain hour, shut off valve B2, gasoline liquid remains in the bottom of gas-liquid separator 9 again.At this moment, because gasoline groove 12 is set, flow into gas-liquid separator 9 so can prevent gasoline vapor, can prevent that high-concentration gasoline steam from flowing into adsorption-desorption tower 7 or adsorption-desorption tower 8 and the cripeturaization (cripetura of switching timing) of the absorption break through of the adsorption-desorption tower 7 that produces and adsorption-desorption tower 8.
That is, in gasoline groove 12, retain a certain amount of gasoline liquid in the bottom, the gasoline liquid that is separated by gas-liquid separator 9 flows into from the bottom, flows from bottom to top.Thus, in gasoline groove 12, become the structure that has gasoline vapor on top.For this reason, when opening valve B2, gasoline vapor can not prevent that the gasoline vapor of high concentration from delivering to adsorption-desorption tower 7 or adsorption-desorption tower 8 against the gas-liquid separator of inflow fluidly 9 of gasoline liquid yet.
Then, the gasoline vapor about the 10vol% that is not handled by condenser pipe 3 is delivered to adsorption-desorption tower 7 or adsorption-desorption tower 8 is handled.In Fig. 1, the situation that expression adsorption-desorption tower 7 moves as desorber as adsorption tower action, adsorption-desorption tower 8.Therefore, solution smokes valve B3 and is open (blacking) state, solution smokes valve B3 ' for closing (blank) state, absorption is open (blacking) state with dump valve B4, absorption uses dump valve B4 ' for closing (blank) state, absorption is open (blacking) state with flowing into valve B6, and absorption is with flowing into valve B6 ' for closing (blank) state.
After the adsorption treatment of being carried out random time by adsorption-desorption tower 7, use as desorber.In this case, solution smokes valve B3 and is made as and closes, and solution smokes valve B3 ' and is made as opening, and absorption is made as with dump valve B4 and closes, and absorption use dump valve B4 ' to be made as opening, and absorption is made as with inflow valve B6 and closes, and adsorbs with inflow valve B6 ' to be made as opening, uses.And then, when gasoline desorb in adsorption-desorption tower 7 finishes, be re-used as adsorption tower and use, carry out this in time repeatedly and move and used.The switching of absorption, desorb as mentioned above, by solution smoke valve B3 and solution smoke valve B3 ', absorption with dump valve B4 and absorption dump valve B4 ', absorption with inflow valve B6 and adsorb with the switching of inflow valve B6 ' and control.
Under the situation of Fig. 1, gasoline vapor conducting and deliver to adsorption-desorption tower 7 in gasoline vapor carrier pipe 14.At adsorption-desorption tower 7 and adsorption-desorption tower 8, enclose the adsorbent that absorbing gasoline steam is arranged.As the adsorbent of gasoline vapor, used silica gel, particularly to have the silica gel in aperture of 4～100 dusts or independent material or their mixture of synthetic zeolite be effective.By making gasoline vapor this adsorbent of flowing through, gasolene ingredient is removed in absorption, and becoming gasoline concentration is the following pure air of 1vol%, by means of the discharge pipe 15 that purifies air discharged to atmosphere.
In addition, set the pressure controller 13 that the pressure discharged to the pure air of atmosphere is controlled to be setting at the discharge pipe 15 that purifies air, this pressure controller 13 will be maintained setting as the pressure in the adsorption-desorption tower 7 of adsorption tower work when being located at pure air discharged to atmosphere.In the gasoline vapor retracting device 100 of present embodiment 1, because use the discharge gas of the high pressure (about 0.3MPa) of condenser pipe 3 to come absorbing gasoline steam, can significantly improve adsorption capacity so compare with absorption under normal pressure.
Adsorption-desorption tower 7 and adsorption-desorption tower 8 are irrelevant with the adsorption-desorption effect of gasoline vapor, are cooled to uniform temperature by the thermal medium of being supplied with by liquid circulation pump 10 all the time.That is, the cooling system of condenser pipe 3, adsorption-desorption tower 7 and adsorption-desorption tower 8 moves control all the time to maintain design temperature.This be because, be filled into the adsorbent of adsorption-desorption tower 7 and adsorption-desorption tower 8 by cooling off from the heat transfer that is located at the fin tube type heat exchanger in adsorption-desorption tower 7 and the adsorption-desorption tower 8, so be absolutely necessary cool time to a certain degree, and can not corresponding instantaneous operation.
In addition, also because, can bring adverse effect to equipment cost in order to be provided with the big refrigerator of cooling capacity 6 in the short time cooling, cheap gasoline vapor retracting device can not be provided.In addition, by reducing adsorption-desorption tower 7 and adsorption-desorption tower 8 temperature inside, can increase the adsorption capacity of adsorbent, reduce the use amount of adsorbent.And then, can also prevent since when stopping to reclaim gasoline vapor the temperature of the adsorbent in adsorption-desorption tower 7 and the adsorption-desorption tower 8 rise and cause gasoline vapor from being filled into adsorbent desorb in adsorption-desorption tower 7 and the adsorption-desorption tower 8, causing the situation of the pressure rising in adsorption-desorption tower 7 and the adsorption-desorption tower 8.
Then, the desorption process to gasoline vapor describes.To when being filled into the adsorbed gasoline of adsorbent as the adsorption-desorption tower 8 of desorber work and carrying out desorb, by driving suction pump 11, attract gases by means of Purge gas discharge pipe 17 from adsorption-desorption tower 8, from adsorbent desorb gasoline.At this moment, solution smokes valve and is made as open (blacking) state, and solution smokes valve B3 ' and is made as (blank) state of closing.Adsorption-desorption tower as adsorption tower performance function during absorption moves under the high pressure conditions of 0.3MPa, and reduces pressure below atmospheric pressure, so by this pressure differential the adsorbed gasoline of the adsorbent of desorber is carried out desorb with suction pump 11 when desorb.
The gasoline vapor of desorb is got back to condenser pipe 3 in Fig. 1, gasolene ingredient returns adsorption-desorption tower 7 after condensation is reclaimed again again.Carry out repeatedly this operation during, the recovery that in condenser pipe 3, is condensed of the gasoline of all amounts.In addition, when desorb, by improving adsorption-desorption tower 8 temperature inside, can accelerate desorption rate, but by reducing temperature, exist the consumed energy in the heating arrangements of refrigerator 6 and heater etc. to increase, can not switch problems such as adsorption-desorption tower 7 and adsorption-desorption tower 8 in the short time simultaneously, so do not improve temperature when desorb, to carry out desorb be effective to identical temperature with absorption the time.
For only being the desorption method that utilizes the pressure differential that the attraction by suction pump 11 produces, because its efficient is not very high, be effective so import Purge gas from the outside.Therefore, in present embodiment 1, will deliver to adsorption-desorption tower 8 discharged to the part of the clean gas of atmosphere by Purge gas inflow pipe 16 from adsorption-desorption tower 7 as this Purge gas and be used.The gas flow of this Purge gas is by mass flow controller B5 and mass flow controller B5 ' control.
In this case, mass flow controller B5 open (blacking) and be in the state of negotiable ormal weight gas, mass flow controller B5 ' closes (blank) and becomes the immobilising state of gas.In addition, in present embodiment 1, because in the condenser pipe 3 of leading portion, the amount of moisture in the gas is fully reduced, so the contained moisture of Purge gas does not almost have adverse effect to the adsorbent in the adsorption-desorption tower 8.In addition, the result who carries out desorption experiment shows, is set at the Purge gas flow under the situation of 15～25L/min, can be made as 15～30kPa to the pressure in the adsorption tower, effectively the desorb gasoline vapor.
In fuel feeding such as gas station were arranged, fuel feeding irregularly carried out.For this reason, from reducing the viewpoint of electricity usage amount, time chien shih gasoline vapor suction pump 2 actions when being only limited to fuel feeding, near the gasoline vapor that reclaims the fuel feeding portion of fueller 1 is desirable.In addition, can make suction pump 11 work in advance corresponding to the work of gasoline vapor suction pump 2.Therefore, the desorb operation of the adsorption operations of the condensation operation of the gasoline vapor that is undertaken by condenser pipe 3, the gasoline vapor that undertaken by adsorption-desorption tower 7 and the gasoline vapor that undertaken by adsorption-desorption tower 8 becomes operation intermittently.By carrying out such system's control, can be reduced in the energy consumption under fueller 1 off position, can realize saving the gasoline vapor retracting device 100 of energy.
At last, the cooling control method of condenser pipe 3 and adsorption-desorption tower 7 and adsorption-desorption tower 8 is set forth.As mentioned above, in condenser pipe 3, freezing in condenser pipe 3 in order to prevent water contained in the gas, is desirable about being made as the design temperature that is stored in the thermal medium in the condenser pipe cooling bath 20 from 0 ℃ to 5 ℃.In addition, for the size that makes adsorption tower is as far as possible little, the temperature that makes adsorbent low (for example under the freezing point) as far as possible is desirable.Therefore, think by the chilling temperature of condenser pipe 3 and adsorption-desorption tower 7 and adsorption-desorption tower 8 is set at different temperature, compared with prior art can carry out high efficiency gasoline and reclaim.
Namely, think and be set in condenser pipe 3 and adsorption-desorption tower 7 and adsorption-desorption tower 8 different by the quantity delivered that use refrigerator 6 and heat exchanger 5 is cooled to the thermal medium of set point of temperature, can can reclaim gasoline expeditiously condenser pipe 3 and adsorption- desorption tower 7 and 8 controls of adsorption-desorption tower in different temperatures.In addition, by the triple valve C1～triple valve C4 of control as the stream switching mechanism, can make the quantity delivered of thermal medium different with adsorption-desorption tower 7 and adsorption-desorption tower 8 at condenser pipe 3.
The cooling control method of adsorption-desorption tower 7 and adsorption-desorption tower 8 at first, is described.Be provided with heat exchanger 5 at thermal medium accumulator tank 4, with the mode store heat medium of these heat exchanger 5 abundant dippings.When refrigerator 6 work, by means of heat exchanger 5 thermal medium in the thermal medium accumulator tank 4 is cooled to set point of temperature.At this moment, also can measure the temperature of thermal medium, by the operation of its signal controlling refrigerator 6.The thermal medium that is cooled to set point of temperature is supplied to adsorption-desorption tower 7 and adsorption-desorption tower 8 by liquid circulation pump 10.Be supplied to the thermal medium of adsorption-desorption tower 7 and adsorption-desorption tower 8, after giving low-temperature heat quantity to adsorption-desorption tower 7 and adsorption-desorption tower 8, turn back to again in the thermal medium accumulator tank 4.
Like this, the adsorbent in adsorption-desorption tower 7 and the adsorption-desorption tower 8 is cooled to set point of temperature.Irrelevant with the action of fueller 1, irrelevant with the effect of the adsorption-desorption of gasoline vapor in addition, all the time thermal medium is supplied to the big adsorption-desorption tower 7 of thermal capacity and adsorption-desorption tower 8 by liquid circulation pump 10.Thus, also can flow into by fully corresponding load intermittently, can realize the gasoline vapor retracting device 100 that reliability is high.In addition, the chilling temperature of adsorbent is reduced to when characterization of adsorption is judged as far as possible, and in order to realize this setting, the chilling temperature of thermal medium also is reduced to as far as possible.
But when the temperature that makes thermal medium was low, because the viscosity of thermal medium increases, the consumed energy of liquid circulation pump 10 increased.In addition, because be used for the deterioration of efficiency of the refrigerator 6 of heat of cooling medium, the consumed energy of refrigerator 6 increases.Therefore, to be set in-20 ℃～0 ℃ be desirable to the chilling temperature of adsorbent.
According to above scheme, by the chilling temperature of adsorption-desorption tower 7 and adsorption-desorption tower 8 is set at-20 ℃～0 ℃, can improve the adsorption efficiency of adsorbent, can obtain compactness and the gasoline vapor retracting device 100 of the condensation gasoline that can liquefy effectively.
The cooling control method of condenser pipe 3 then, is described.Identical with the situation of adsorption-desorption tower 7 and adsorption-desorption tower 8, the thermal medium that is cooled to set point of temperature is supplied to condenser pipe cooling bath 20 by liquid circulation pump 10 by means of thermal medium supply control valve B7.In condenser pipe cooling bath 20, be stored in the thermal medium of condenser pipe cooling bath 20 and the thermal medium mixing of supplying with from thermal medium accumulator tank 4.This thermal medium obtains the heat that produces from condenser pipe 3, returns in the thermal medium accumulator tank 4 again.At this moment, utilize temperature measuring device 19 to measure the temperature of the exit gas of condenser pipes 3 so that its temperature not the mode under freezing point open and close thermal medium and supply with control valve B7, control is supplied to the thermal medium amount of condenser pipe cooling bath 20.
Like this, the air that contains gasoline vapor that flows in condenser pipe 3 is cooled to set point of temperature above freezing.Thus, the moisture in the gas does not freeze, effectively liquified petroleum steam.As mentioned above, supply with the thermal medium that is cooled to adsorption-desorption tower 7 and adsorption-desorption tower 8 all the time by liquid circulation pump 10, but condenser pipe cooling bath 20 and the action of fueller 1 are supplied with thermal mediums by liquid circulation pump 10 with coincideing.That is, because condenser pipe 3 is made of metal, so the heat conduction is fast, can cool off faster, so coincide with the action of fueller 1, before the gas temperature of condenser pipe 3 outlets reaches setting, supply with thermal mediums by liquid circulation pump 10.
In addition, in present embodiment 1, connect to supply with control valve B7 by the switch thermal medium that to disconnect the situation that control is supplied to the thermal medium amount of condenser pipe cooling bath 20 be that example is represented, but also can carry out flow-control to the flow self of thermal medium.By like this, can control the temperature of the thermal medium in the condenser pipe cooling bath 20 more to heavens.
According to above scheme, by the chilling temperature of condenser pipe 3 is set at temperature above freezing, can prevents from producing at condenser pipe 3 and freeze, it is high and can reclaim the gasoline vapor retracting device 100 of gasoline effectively to obtain reliability.
, because the work of fueller 1 is intermittently, so when fuel feeding finished, fueller 1 stopped.In this case, make by adsorbent gasoline desorb discharged in the atmosphere in order to prevent from being reduced by the pressure of adsorption-desorption tower 7, valve B1, valve B2, solution smoke valve B3, absorption with dump valve B4, mass flow controller B5 and absorption with flowing into valve B6 Close All.In addition, as mentioned above, because supply with thermal medium all the time at adsorption-desorption tower 7 and adsorption-desorption tower 8, the situation that the pressure in gasoline vapor desorb, adsorption-desorption tower 7 and the adsorption-desorption tower 8 rises so can not take place in the cooling adsorbent.
In addition, in this case, also can smoke valve B3 and solution smokes valve B3 ' by the open solution of being located at adsorption-desorption tower 7 and adsorption-desorption tower 8 bottoms, the gasoline vapor that is adsorbed on adsorption-desorption tower 7 bottoms is transferred to the bottom of adsorption-desorption tower 8, make the pressure of adsorption-desorption tower 7 identical with the pressure of adsorption-desorption tower 8 simultaneously, relax the rising of pressure thus.Thus, under fueller 1 idle state, also can reduce energy consumption as far as possible, can prevent that the pressure of gasoline vapor retracting device 100 from rising simultaneously, can realize the gasoline vapor retracting device 100 that reliability is high.
In present embodiment 1, utilize temperature measuring device 19 to measure the gas temperature of condenser pipe 3 outlets, control is supplied to the thermal medium amount of condenser pipe cooling bath 20, but also can measure the pressure differential of gasoline vapor of the gateway of condenser pipes 3 with the difference gauge 21 of embodiment 2 described later, control is supplied to the thermal medium amount of condenser pipe cooling bath 20.In this case, as long as the quantity delivered of control thermal medium is so that the pressure differential of being measured by difference gauge 21 becomes authorized pressure.In addition, in present embodiment 1, measure the gas temperature of condenser pipe 3 outlets by temperature measuring device 19, control is supplied to the thermal medium amount of condenser pipe cooling bath 20, but also can utilize temperature measuring device 19 to measure the temperature of thermal medium in part from thermal medium to condenser pipe cooling bath 20 that supply with.
And then, measure by the temperature at position that the thermal medium that is stored in the condenser pipe cooling bath 20 is mixed with the thermal medium of being supplied with by liquid circulation pump 10, in the time of can realizing obtaining with the gas temperature measured in the condenser pipe 3 substantially the temperature of equal performance control.At this, owing to carry out the temperature survey at the position of the different thermal medium mixing of temperature, must under the relatively fiercer state that changes of the temperature of thermal medium, measure the temperature of thermal medium, judge that thermal medium reaches the words of design temperature, with measure condenser pipe 3 in the situation of the gas temperature difficulty of comparing, compare with gas temperature mensuration modes in the condenser pipe 3 and to be in a disadvantageous position.
Fig. 2 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 2.Based on Fig. 2 formation and the action of the processing retracting device (the following gasoline vapor retracting device 200 that is called simply) of vaporous hydrocarbon are described.The gasoline vapor retracting device of this gasoline vapor retracting device 200 and embodiment 1 equally when supplying with gasoline to discharged to the liquefaction of the gasoline in the gasoline vapor in the atmosphere and reclaim.In addition, in embodiment 2, by with the difference of embodiment 1 centered by describe, to the identical Reference numeral of the part mark identical with embodiment 1 and omit explanation.
In embodiment 1, be that example is illustrated with the gas temperature of measuring condenser pipes 3 outlets with temperature measuring device 19, the situation that control is supplied to the thermal medium amount of condenser pipe cooling bath 20, but in present embodiment 2, be to measure the pressure differential of the entrance and exit of condenser pipes 3 with difference gauge 21, to be its value that example describes with setting value the situation that compares to control the thermal medium amount that is supplied to condenser pipe cooling bath 20.This difference gauge 21 is according to the pressure differential of the gasoline vapor of the entrance and exit of the piezometry condenser pipe 3 of the gasoline vapor of the outlet side of the pressure of the gasoline vapor of the entrance side of condenser pipe 3 and condenser pipe 3.In addition, the pressure differential information by difference gauge 21 is measured is transported to diagram abridged control device as signal.
Thus, because the moisture in the gas freezes in condenser pipe 3 inside, ice is attached to condenser pipe 3 inside, increases so can directly detect the pressure loss of condenser pipe 3.Therefore, gasoline vapor retracting device 200 can be controlled the thermal medium amount that is supplied to condenser pipe cooling bath 20 more accurately, can provide can be efficient low liquefaction to reclaim the gasoline vapor retracting device 200 of gasoline.In addition, the temperature measuring device 19 that also can make up the gasoline vapor retracting device 100 of embodiment 1 in this gasoline vapor retracting device 200 arranges.Like this, can control the thermal medium amount that is supplied to condenser pipe cooling bath 20 more accurately, recovery gasoline expeditiously can liquefy.
Fig. 3 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 3.Based on Fig. 3 formation and the action of the processing retracting device (the following gasoline vapor retracting device 300 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 300 is same with the gasoline vapor retracting device of embodiment 1 and embodiment 2, when supplying with gasoline contained gasoline in discharged to the gasoline vapor in the atmosphere is liquefied and reclaims.In addition, in embodiment 3, by with the difference of embodiment and embodiment 2 centered by describe, to the identical Reference numeral of the part mark identical with embodiment 1 and embodiment 2 and omit explanation.
In embodiment 1 and embodiment 2, situation about being located in the condenser pipe cooling bath 20 with condenser pipe 3 is that example is illustrated, but in present embodiment 3, except condenser pipe 3, also gas-liquid separator 9 and connect condenser pipe 3 and the pipe arrangement of gas-liquid separator 9 is located at the second thermal medium cooling bath, 31 inside as the thermal medium container, by supply with the thermal medium of cooling to the second thermal medium cooling bath 31, cooling condensation pipe 3, the pipe arrangement of gas-liquid separator 9 and connection condenser pipe 3 and gas-liquid separator 9 prevents from arriving gas-liquid separator 9 evaporation more before by the gasoline liquid of condenser pipe 3 liquefaction thus effectively.That is, by condenser pipe 3 and the second thermal medium cooling bath 31, performance is as the function of the condensing unit of liquified petroleum steam.
Thus, gasoline vapor can be reclaimed effectively, the gasoline vapor of being removed by adsorption-desorption tower 7 and adsorption-desorption tower 8, adsorbent capable of reducing using can be reduced simultaneously.According to above scheme, can provide and save energy and compact gasoline vapor retracting device 300.In addition, in gasoline vapor retracting device 300, be that example is represented with the situation that temperature measuring device 19 is set, but also available and embodiment 2 same difference gauges 21 substitute temperature measuring devices 19, perhaps with temperature measuring device 19 this difference gauge 21 are set simultaneously.
Embodiment 4.
Fig. 4 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 4.Based on Fig. 4 formation and the action of the processing retracting device (the following gasoline vapor retracting device 400 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 400 is same to the gasoline vapor retracting device of embodiment 3 with embodiment 1, when supplying with gasoline contained gasoline in discharged to the gasoline vapor in the atmosphere is liquefied and reclaims.In addition, in embodiment 4, describing to the difference of embodiment 3 with embodiment 1, to embodiment 1 to the identical Reference numeral of the identical part mark of embodiment 3 and omit explanation.
In present embodiment 4, can directly be supplied to condenser pipe cooling bath 20 with being used in the thermal medium that adsorption-desorption tower 7 and adsorption-desorption tower 8 are cooled off.Namely, after thermal medium is supplied to adsorption-desorption tower 7 and adsorption-desorption tower 8 with liquid circulation pump 10, can controls by means of the thermal medium loopback and directly turn back to the situation of thermal medium accumulator tank 4 and supply with the situation that control valve B7 directly is supplied to condenser pipe cooling bath 20 by means of thermal medium with valve B8.This thermal medium loopback is located between triple valve C5 and the triple valve C1 with valve B8, and this triple valve C5 supplies with control valve B7, triple valve C1 with thermal medium and triple valve C2 is connected, and is located between triple valve C1 and the triple valve C2.
Like this, because can be improved the temperature of the thermal medium that is supplied to condenser pipe cooling bath 20 by the heat that produces at adsorption-desorption tower 7, can reduce to be present in the thermal medium of condenser pipe cooling bath 20 originally and to be supplied to the temperature difference of the thermal medium of condenser pipe cooling bath 20, so can carry out more high-precision control to condenser pipe 3 gas inside temperature.Therefore, can provide the gasoline vapor retracting device 400 of liquified petroleum expeditiously.In addition, in gasoline vapor retracting device 400, be that example is represented with the situation that temperature measuring device 19 is set, but also available and embodiment 2 same difference gauges 21 substitute temperature measuring devices 19, perhaps with temperature measuring device 19 this difference gauge 21 are set simultaneously.
Fig. 5 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 5.Based on Fig. 5 formation and the action of the processing retracting device (the following gasoline vapor retracting device 500 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 500 is same to the gasoline vapor retracting device of embodiment 4 with embodiment 1, when supplying with gasoline contained gasoline in discharged to the gasoline vapor in the atmosphere is liquefied and reclaims.In addition, in embodiment 5 describing to the difference of embodiment 4 with embodiment 1, to embodiment 1 to the identical Reference numeral of the identical part mark of embodiment 4 and omit explanation.
In present embodiment 5, between thermal medium supply control valve B7 and condenser pipe cooling bath 20, arrange on thermoregulator 41 this point different with embodiment 4.Thus, because can set the temperature that is supplied to the thermal medium of condenser pipe cooling bath 20 to such an extent that compare from the temperature height of the thermal medium of adsorption-desorption tower 7 and the 8 outlet discharges of adsorption-desorption tower with thermoregulator 41, can reduce to be present in the thermal medium of condenser pipe cooling bath 20 originally and to be supplied to the temperature difference of the thermal medium of condenser pipe cooling bath 20, so can control condenser pipe 3 gas inside temperature more accurately.According to above scheme, can provide the gasoline vapor retracting device 500 of liquified petroleum efficiently.In addition, in gasoline vapor retracting device 500, be that example is represented with the situation that temperature measuring device 19 is set, but also available and embodiment 2 same difference gauges 21 substitute temperature measuring devices 19, perhaps with temperature measuring device 19 this difference gauge 21 are set simultaneously.
Fig. 6 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 6.Based on Fig. 6 formation and the action of the processing retracting device (the following gasoline vapor retracting device 600 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 600 is same to the gasoline vapor retracting device of embodiment 5 with embodiment 1, when supplying with gasoline to liquefying discharged to the gasoline in the gasoline vapor in the atmosphere and reclaiming.In addition, in embodiment 6 describing to the difference of embodiment 5 with embodiment 1, to embodiment 1 to the identical Reference numeral of the identical part mark of embodiment 5 and omit explanation.
In present embodiment 6, condenser pipe 3 and condenser pipe cooling bath 20 are being replaced with condensation with heat exchanger 52 and to hold this condensation different to embodiment 5 with embodiment 1 with condensing container 51 this point of heat exchanger 52.That is, with heat exchanger 52 and condensing container 51, bring into play the function as the condensing unit of liquified petroleum steam by condensation.In addition, as condensation with heat exchanger 52, the pressure loss little aspect or can cool off the aspect of the gas that contains gasoline vapor effectively, use fin tube type heat exchanger to be best suited for.In addition, condensing container 51 is so long as can deposit condensation with the container of heat exchanger 52 in inside, and just there is no particular limitation to kind.
Action to gasoline vapor retracting device 600 describes simply.When the work while gasoline vapor suction pump 2 with fueller 1 begins to move, suck gasoline vapor, supply gas with the condensing container 51 of heat exchanger 52 to holding condensation.The gasoline vapor of delivering in the condensing container 51 flows in condensing container 51, liquefies with heat exchanger 52 surfaces in condensation.Supply with control valve B7 by means of thermal medium and supply with thermal medium to condensation with heat exchanger 52 by liquid circulation pump 10.By this thermal medium, the gasoline vapor of delivering to condensing container 51 is cooled.
At this moment, as mentioned above, the gas temperature by with 51 outlets of temperature measuring device 19 measurement condensing containers opens and closes thermal medium and supply with control valve B7, thereby control is supplied to the thermal medium amount that heat exchanger 52 is used in condensation.Thus, can prevent from taking place with the situation of the interlobate gas flow path of heat exchanger 52 with the moisture freezes in heat exchanger 52 surface gas, obstruction condensation in condensation.According to above scheme, can provide reliability high and can reclaim the gasoline vapor retracting device 600 of gasoline effectively.In addition, in gasoline vapor retracting device 600, be that example is represented with the situation that temperature measuring device 19 is set, but also available and embodiment 2 same difference gauges 21 substitute temperature measuring devices 19, perhaps with temperature measuring device 19 this difference gauge 21 are set simultaneously.In addition, the thermal medium loopback valve B8 same with embodiment 4 also can be set.
Fig. 7 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 7.Based on Fig. 7 formation and the action of the processing retracting device (the following gasoline vapor retracting device 700 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 700 is same to the gasoline vapor retracting device of embodiment 6 with embodiment 1, when supplying with gasoline to liquefying discharged to the gasoline in the gasoline vapor in the atmosphere and reclaiming.In addition, in embodiment 7 describing to the difference of embodiment 6 with embodiment 1, to embodiment 1 to the identical Reference numeral of the identical part mark of embodiment 6 and omit explanation.
In present embodiment 7, it is different with embodiment 6 to have added metallic particles 53 this point in being provided with the condensing container 51 of condensation with heat exchanger 52.Metallic particles 53 conducts, is not subjected to the aluminium of corrosion such as gasoline vapor or copper etc. to be fit to for heat.Like this, because can in condensing container 51, cool off gasoline vapor effectively, so liquified petroleum steam effectively.In addition, can make the structure of condensing container 51 identical with the structure of adsorption-desorption tower 7 and adsorption-desorption tower 8, be made as adsorbent or metallic particles 53 by the object that will fill in inside, can make the container part generalization.
According to above scheme, can provide cheap, the gasoline vapor retracting device 700 of liquified petroleum expeditiously.In addition, in gasoline vapor retracting device 700, be that example is represented with the situation that temperature measuring device 19 is set, but also available and embodiment 2 same difference gauges 21 substitute temperature measuring devices 19, perhaps with temperature measuring device 19 this difference gauge 21 are set simultaneously.In addition, the thermal medium loopback valve B8 same with embodiment 4 also can be set.And then metallic particles 53 is not limited to aluminium or copper as long as conducted, not constituted by the material of corrosion such as gasoline vapor by heat.
Fig. 8 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 8.Based on Fig. 8 formation and the action of the processing retracting device (the following gasoline vapor retracting device 800 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 800 is same to the gasoline vapor retracting device of embodiment 7 with embodiment 1, when supplying with gasoline contained gasoline in discharged to the gasoline vapor in the atmosphere is liquefied and reclaims.In addition, in embodiment 8 describing to the difference of embodiment 7 with embodiment 1, to embodiment 1 to the identical Reference numeral of the identical part mark of embodiment 7 and omit explanation.
At embodiment 1 to embodiment 7, all the time in adsorption-desorption tower 7 and adsorption-desorption tower 8 supply thermal mediums, measuring the gas temperature of condenser pipe 3 outlets with temperature measuring device 19 (perhaps difference gauge 21), control is supplied to the thermal medium amount of condenser pipe cooling bath 20, but in present embodiment 8, supply with control valve B9 and three thermal medium supply control valve B10 by control as second thermal medium of thermal medium supply control valve for adsorption-desorption tower 7 and adsorption-desorption tower 8, all the time only the adsorption-desorption tower 7 as adsorption tower work is supplied with thermal medium, simultaneously to limit the quantity delivered of thermal mediums as the adsorption-desorption tower 8 of desorber work.
Second thermal medium is supplied with control valve B9 and is located in the pipe arrangement between triple valve C4 and the adsorption-desorption tower 7, and the 3rd thermal medium is supplied with control valve B10 and is located in the pipe arrangement between triple valve C4 and the adsorption-desorption tower 8.Thus, can improve the temperature as the adsorption-desorption tower 8 of desorber work, can be effectively from adsorption-desorption tower 8 desorb gasoline vapors, so can adsorb fully in the time spent of doing of switching adsorption-desorption tower 7 and adsorption-desorption tower 8.Therefore, can provide temperature, adsorption-desorption tower 7 and adsorption-desorption tower 8 compactnesses that to control adsorption-desorption tower 7 and adsorption-desorption tower 8, the gasoline vapor retracting device 800 that can liquefy recovery gasoline expeditiously.
In addition, in present embodiment 8, represented when the condensation part has (condenser pipe 3 and condenser pipe cooling bath 20), an adsorption-desorption tower that two (adsorption-desorption tower 7 and adsorption-desorption towers 8) are arranged, controlled the situation of temperature separately respectively by the amount of controlling the thermal medium of supplying with to them respectively, but also can use the same method, control is supplied to the thermal medium amount of a plurality of condensation parts and a plurality of adsorption-desorption towers.Like this, can control the temperature of a plurality of condensation parts and a plurality of adsorption-desorption towers individually, effectively liquified petroleum.
In addition, in gasoline vapor retracting device 800, be that example is represented with the situation that temperature measuring device 19 is set, but also available and embodiment 2 same difference gauges 21 substitute temperature measuring devices 19, perhaps with temperature measuring device 19 this difference gauge 21 are set simultaneously.In addition, the thermal medium loopback valve B8 same with embodiment 4 also can be set.And then, also can substitute condenser pipes 3 equally and adopt condensation heat exchanger 52 with embodiment 6 and embodiment 7.In this case, can be in condensing container 51 filling metallic particles for overlay 53.
Fig. 9 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 9.Based on Fig. 9 formation and the action of the processing retracting device (the following gasoline vapor retracting device 900 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 900 is same to the gasoline vapor retracting device of embodiment 8 with embodiment 1, when supplying with gasoline contained gasoline in discharged to the gasoline vapor in the atmosphere is liquefied and reclaims.In addition, in embodiment 9 describing to the difference of embodiment 8 with embodiment 1, to embodiment 1 to the identical Reference numeral of the identical part mark of embodiment 8 and omit explanation.
In present embodiment 9, at the gas vent of gas-liquid separator 9 second pressure controller 61 is set, only to improve condenser pipe 3 pressure inside this point different to embodiment 8 with embodiment 1.Because the gas vent at gas-liquid separator 9 arranges second pressure controller 61, so can set De Genggao to the pressure inside of condenser pipe 3.Thus, owing to can make the gasoline vapor concentration of condenser pipe 3 outlets lower, can reduce the gasoline concentration that is supplied to adsorption-desorption tower 7 and adsorption-desorption tower 8, so can dwindle adsorption-desorption tower 7 and adsorption-desorption tower 8.In addition, also can improve gas-liquid separator 9 pressure inside by second pressure controller 61.
Because condenser pipe 3 is to be wound in spiral helicine pipe arrangement, can improve pressure so needn't just handle as pressure vessel.In addition, because adsorption-desorption tower 7 and adsorption-desorption tower 8 are pressure vessels, so when improving pressure, must make withstand voltage structure, container cost improves.Therefore, by only improving the pressure of condenser pipe 3, the interior pressure of adsorption-desorption tower 7 and adsorption-desorption tower 8 is made as not below the 0.3MPa that handles as pressure vessel, can makes the device cheapness.By above formation, can provide cheap, compact and the gasoline vapor retracting device 900 of liquified petroleum expeditiously.
In addition, according to gasoline vapor retracting device 900, be provided as second pressure controller 61 of pressure-control valve by the back segment at gas-liquid separator 9, can improve condenser pipe 3 pressure inside and gas-liquid separator 9 pressure inside as condensing unit, the saturated evaporative concn of the organic carbon hydrogen compound of the butane that is difficult to liquefy so can reduce the boiling point height or pentane etc., at condenser pipe 3 low-boiling organic carbon hydrogen compound such as liquefied butane or pentane effectively, improve the organic efficiency of gasoline vapor.And then, according to gasoline vapor retracting device 900, by adsorbance not the adsorption-desorption tower 7 that increases of corresponding pressure and the pressure of adsorption-desorption tower 8 remain on below the authorized pressure, needn't set the compression resistance of adsorption-desorption tower 7 and adsorption-desorption tower 8 too highly, can reduce cost.
In addition, in gasoline vapor retracting device 900, be that example is represented with the situation that temperature measuring device 19 is set, but also available and embodiment 2 same difference gauges 21 substitute temperature measuring devices 19, perhaps with temperature measuring device 19 this difference gauge 21 are set simultaneously.In addition, the thermal medium loopback valve B8 same with embodiment 4 also can be set.And then, also can substitute condenser pipes 3 equally and adopt condensation heat exchanger 52 with embodiment 6 and embodiment 7.In this case, can be in condensing container 51 filling metallic particles for overlay 53.
Figure 10 is the whole pie graph of flow process of processing retracting device of the vaporous hydrocarbon of expression embodiments of the present invention 10.Based on Figure 10 formation and the action of the processing retracting device (the following gasoline vapor retracting device 1000 that is called simply) of vaporous hydrocarbon are described.This gasoline vapor retracting device 1000 is same to the gasoline vapor retracting device of embodiment 9 with embodiment 1, when supplying with gasoline contained gasoline in discharged to the gasoline vapor in the atmosphere is liquefied and reclaims.In addition, in embodiment 10 describing to the difference of embodiment 9 with embodiment 1, to embodiment 1 to the identical Reference numeral of the identical part mark of embodiment 9 and omit explanation.
In present embodiment 10, flow totalizer 71 being arranged at discharge pipe 15 this point of sending to atmosphere from the air of adsorption- desorption tower 7 or 8 discharges of adsorption-desorption tower that purify air, different to embodiment 9 with embodiment 1.Thus, can accurately measure from the cumulant of the gas of adsorption- desorption tower 7 or 8 discharges of adsorption-desorption tower, accurately implement the switching of adsorption-desorption tower 7 or adsorption-desorption tower 8.Therefore, can dwindle the capacity of adsorption-desorption tower 7 and adsorption-desorption tower 8 to greatest extent, have the densification of device integral body, maybe can realize prolonging the switching time of adsorption-desorption tower 7 adsorption-desorption towers 8, the effect of device long lifetime that prolongs service life etc. of valve.
Therefore, according to gasoline vapor retracting device 1000, because the discharge pipe 15 that purifies air that is connected in the outlet with adsorption-desorption tower 7 and adsorption-desorption tower 8 arranges flow totalizer 71, so can clearly understand the air total amount through adsorption-desorption tower 7 and adsorption-desorption tower 8, the petrol-depth gauge of high price need not be set, just can clear and definite adsorption-desorption tower 7 and the function of adsorption-desorption tower 8 reverse, be adsorption tower and the switching timing of taking off tower.In addition, can dwindle the capacity of adsorption-desorption tower 7 and adsorption-desorption tower 8 to greatest extent, the densification of implement device integral body.
In addition, in gasoline vapor retracting device 1000, be that example is represented with the situation that temperature measuring device 19 is set, but also available and embodiment 2 same difference gauges 21 substitute temperature measuring devices 19, perhaps with temperature measuring device 19 this difference gauge 21 are set simultaneously.In addition, the thermal medium loopback valve B8 same with embodiment 4 also can be set.And then, also can substitute condenser pipes 3 equally and adopt condensation heat exchanger 52 with embodiment 6 and embodiment 7.In this case, can be in condensing container 51 filling metallic particles for overlay 53.In addition, also can set second pressure controller 61 same with embodiment 9.
Claims (10)
1. the processing retracting device of a vaporous hydrocarbon, the processing retracting device of this vaporous hydrocarbon are used for gasoline vapor is handled, reclaimed, and it is characterized in that possessing:
Condensing unit, this condensing unit liquefies gasoline vapor,
Gas-liquid separator, this gas-liquid separator will be separated with gasoline vapor by the gasoline liquid of described condensing unit liquefaction,
The adsorption-desorption device, this adsorption-desorption device carries out adsorption-desorption to the gasoline vapor by described gas-liquid separator separates,
The thermal medium accumulator tank, this thermal medium accumulator tank stores the thermal medium of the described condensing unit of cooling and described adsorption-desorption device,
The thermal medium that liquid circulation pump, this liquid circulation pump will be stored in the described thermal medium accumulator tank is supplied to described condensing unit and described adsorption-desorption device,
Refrigerator, this refrigerator cooling is stored in the thermal medium in the described thermal medium accumulator tank,
Valve, this valve adjustment be supplied to described condensing unit the thermal medium amount and
The temperature at the position that control device, this control device mix mutually according to the thermal medium and the thermal medium by described liquid circulation pump supply that are stored in the described condensing unit is controlled the switching of described valve.
2. the processing retracting device of a vaporous hydrocarbon, the processing retracting device of this vaporous hydrocarbon are used for gasoline vapor is handled, reclaimed, and it is characterized in that possessing:
Condensing unit, this condensing unit liquefies gasoline vapor,
Gas-liquid separator, this gas-liquid separator will be separated with gasoline vapor by the gasoline liquid of described condensing unit liquefaction,
The adsorption-desorption device, this adsorption-desorption device carries out adsorption-desorption to the gasoline vapor by described gas-liquid separator separates,
The thermal medium accumulator tank, this thermal medium accumulator tank stores the thermal medium of the described condensing unit of cooling and described adsorption-desorption device,
The thermal medium that liquid circulation pump, this liquid circulation pump will be stored in the described thermal medium accumulator tank is supplied to described condensing unit and described adsorption-desorption device,
Refrigerator, this refrigerator cooling is stored in the thermal medium in the described thermal medium accumulator tank,
Valve, this valve adjustment is supplied to the thermal medium amount of described condensing unit,
Difference gauge, this difference gauge measure described condensing unit gateway place gasoline vapor pressure differential and
Control device, this control device receives the switching of controlling described valve from the signal of described difference gauge.
3. the processing retracting device of vaporous hydrocarbon as claimed in claim 1 or 2 is characterized in that, described condensing unit comprises:
Pipe arrangement is used in cooling, this cooling with pipe arrangement make the gasoline vapor conducting and
The thermal medium container, this thermal medium container possesses described cooling pipe arrangement in inside, can store the thermal medium of supplying with from described thermal medium accumulator tank.
4. the processing retracting device of vaporous hydrocarbon as claimed in claim 1 or 2 is characterized in that, at the back segment of described gas-liquid separator, is provided with the pressure inside pressure-control valve higher than the pressure of described adsorption-desorption device that makes described cooling use pipe arrangement.
5. the processing retracting device of vaporous hydrocarbon as claimed in claim 1 or 2 is characterized in that, described condensing unit comprises:
Heat exchanger, the thermal medium of supplying with from described thermal medium accumulator tank flow through this heat exchanger and
Condensing container, this condensing container hold described heat exchanger in inside, gasoline vapor can flow through this condensing container.
6. the processing retracting device of vaporous hydrocarbon as claimed in claim 1 or 2 is characterized in that, the thermal medium that is supplied to described adsorption-desorption device from described thermal medium accumulator tank can be supplied to described condensing unit.
7. the processing retracting device of vaporous hydrocarbon as claimed in claim 6, it is characterized in that, between described adsorption-desorption device and described condensing unit, be provided with the thermoregulator that the temperature of the thermal medium to described condensing unit supply from described adsorption-desorption device is regulated.
8. the processing retracting device of vaporous hydrocarbon as claimed in claim 1 or 2 is characterized in that, possesses two described adsorption-desorption devices, and one as adsorption tower work, and another is as desorber work, wherein,
In the pipe arrangement that connects described thermal medium accumulator tank and described adsorption-desorption tower, be provided with thermal medium and supply with control valve,
Supply with the switching of control valve by controlling described thermal medium, the adsorption-desorption device as adsorption tower work is continued to supply with thermal medium, and thermal medium is supplied with in the adsorption-desorption device restriction as desorber work.
9. the processing recovery method of a vaporous hydrocarbon, in the processing recovery method of this vaporous hydrocarbon,
The attraction gasoline vapor also pressurizes,
By condensing unit with this gasoline vapor cooling liquid,
To be separated with gasoline vapor by the gasoline liquid of described condensing unit liquefaction,
By the adsorption-desorption device gasoline vapor that separates is carried out adsorption-desorption,
Be used for the thermal medium of cooling gasoline vapor to described condensing unit and described adsorption-desorption unit feeding,
Utilize refrigerator to cool off described thermal medium, it is characterized in that,
By liquid circulation pump always to the thermal medium of described adsorption-desorption unit feeding cooling, simultaneously
The temperature at the position of mixing mutually according to the thermal medium and the thermal medium of being supplied with by described liquid circulation pump that are stored in the described condensing unit, so that the gas temperature of the outlet of described condensing unit becomes the mode of set point of temperature, supply with the thermal medium of cooling to described condensing unit.
10. the processing recovery method of a vaporous hydrocarbon, in the processing recovery method of this vaporous hydrocarbon,
The attraction gasoline vapor also pressurizes,
By condensing unit with this gasoline vapor cooling liquid,
To be separated with gasoline vapor by the gasoline liquid of described condensing unit liquefaction,
By the adsorption-desorption device gasoline vapor that separates is carried out adsorption-desorption,
Be used for the thermal medium of cooling gasoline vapor to described condensing unit and described adsorption-desorption unit feeding,
Utilize refrigerator to cool off described thermal medium, it is characterized in that,
Always to the thermal medium of described adsorption-desorption unit feeding cooling, simultaneously
So that the pressure differential of the gasoline vapor at place, the gateway of described condensing unit becomes the mode of authorized pressure, supply with the thermal medium of cooling to described condensing unit.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/JP2008/056007 WO2009118876A1 (en) | 2008-03-28 | 2008-03-28 | Gaseous hydrocarbon treating/recovering apparatus and method |
Publications (2)
| Publication Number | Publication Date |
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| CN101970082A CN101970082A (en) | 2011-02-09 |
| CN101970082B true CN101970082B (en) | 2013-08-14 |
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| CN200880128078.4A Expired - Fee Related CN101970082B (en) | 2008-03-28 | 2008-03-28 | Device and method for treating and recovering gaseous hydrocarbon |
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| Country | Link |
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| JP (1) | JP5289427B2 (en) |
| KR (1) | KR101215211B1 (en) |
| CN (1) | CN101970082B (en) |
| TW (1) | TW200940156A (en) |
| WO (1) | WO2009118876A1 (en) |
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| KR101268694B1 (en) * | 2009-03-31 | 2013-05-29 | 가부시키가이샤 다쯔노 | Apparatus and method for recovering gaseous hydrocarbon |
| KR101167207B1 (en) | 2010-11-03 | 2012-07-24 | 세계화학공업(주) | The apparatus for volatile organic compoundsand and method for recovery of volatile organic compounds |
| 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 |
| CN103349885B (en) * | 2013-07-23 | 2015-04-15 | 蔡兵 | Oil steam recovery system and recovery method |
| KR102701361B1 (en) * | 2016-03-18 | 2024-09-02 | 삼성디스플레이 주식회사 | Apparatus for filtering volatile organic compounds and method for filtering volatile organic compounds |
| CN107986222B (en) * | 2016-10-26 | 2020-04-17 | 株式会社龙野 | Oil filling device |
| CN107050912B (en) * | 2017-01-13 | 2022-08-02 | 陕西延长石油（集团）有限责任公司 | Gas-phase condensed liquid recovery system and method |
| CN109200745A (en) * | 2018-08-31 | 2019-01-15 | 江苏新久扬环保设备科技有限公司 | A kind of oil gas absorbing recovery device and technique |
| CN110068488A (en) * | 2019-03-27 | 2019-07-30 | 北京航空航天大学 | A kind of lossless device and method for acquiring semi-volatile organic matter in stationary source flue gas |
| CN113457569B (en) * | 2021-07-28 | 2022-10-04 | 湖北兴瑞硅材料有限公司 | Vacuum device and process suitable for cracking dimethyl dichlorosilane hydrolysate |
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- 2008-03-28 WO PCT/JP2008/056007 patent/WO2009118876A1/en active Application Filing
- 2008-03-28 JP JP2010505103A patent/JP5289427B2/en not_active Expired - Fee Related
- 2008-03-28 CN CN200880128078.4A patent/CN101970082B/en not_active Expired - Fee Related
- 2008-03-28 KR KR1020107019909A patent/KR101215211B1/en active IP Right Grant
- 2008-04-25 TW TW097115218A patent/TW200940156A/en not_active IP Right Cessation
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| CN1265050A (en) * | 1997-05-07 | 2000-08-30 | 株式会社宇宙总合研究所 | Adhesive, process for preparing same, and method for recovering vapor of hydrocarbon by utilizing condensation by cooling |
| US6120581A (en) * | 1999-01-13 | 2000-09-19 | Uop Llc | Sulfur production process |
| 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 |
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Also Published As
| Publication number | Publication date |
|---|---|
| TWI369243B (en) | 2012-08-01 |
| TW200940156A (en) | 2009-10-01 |
| JP5289427B2 (en) | 2013-09-11 |
| KR20100121639A (en) | 2010-11-18 |
| JPWO2009118876A1 (en) | 2011-07-21 |
| CN101970082A (en) | 2011-02-09 |
| WO2009118876A1 (en) | 2009-10-01 |
| KR101215211B1 (en) | 2012-12-24 |
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