WO2009118876A1 - Appareil et procédé de traitement/récupération d’hydrocarbure gazeux - Google Patents

Appareil et procédé de traitement/récupération d’hydrocarbure gazeux Download PDF

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Publication number
WO2009118876A1
WO2009118876A1 PCT/JP2008/056007 JP2008056007W WO2009118876A1 WO 2009118876 A1 WO2009118876 A1 WO 2009118876A1 JP 2008056007 W JP2008056007 W JP 2008056007W WO 2009118876 A1 WO2009118876 A1 WO 2009118876A1
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WIPO (PCT)
Prior art keywords
adsorption
heat medium
gasoline vapor
gasoline
desorption
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Application number
PCT/JP2008/056007
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English (en)
Japanese (ja)
Inventor
猛 杉本
泰宏 谷村
裕之 森本
勝彦 関谷
明 田中
Original Assignee
三菱電機株式会社
株式会社タツノ・メカトロニクス
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Application filed by 三菱電機株式会社, 株式会社タツノ・メカトロニクス filed Critical 三菱電機株式会社
Priority to PCT/JP2008/056007 priority Critical patent/WO2009118876A1/fr
Priority to JP2010505103A priority patent/JP5289427B2/ja
Priority to CN200880128078.4A priority patent/CN101970082B/zh
Priority to KR1020107019909A priority patent/KR101215211B1/ko
Priority to TW097115218A priority patent/TW200940156A/zh
Publication of WO2009118876A1 publication Critical patent/WO2009118876A1/fr

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    • 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

Definitions

  • the present invention relates to an apparatus and method for treating and recovering gaseous hydrocarbons contained in an atmospheric emission gas, and more particularly to an apparatus and method for treating gasoline vapor that leaks during gasoline refueling.
  • the gas generated from the exhaust gas source (exhaust gas containing about 40 vol% gasoline vapor) is blower or self-pressure to the condenser through the exhaust gas feed pipe.
  • Air is fed and air containing gasoline vapor that has not been liquefied after partially liquefying gasoline vapor in the condenser is sent to the adsorption tower, and the treated exhaust gas that has finished the adsorption process is switched to the adsorption tower (desorption process) After that, there is one that is discharged into the atmosphere as air (clean gas) containing 1 vol% or less of gasoline vapor from the top of the adsorption tower) through a discharge pipe.
  • air clean gas
  • the purge gas is supplied to the adsorption tower after the adsorption step through the purge gas supply pipe, and desorption is performed by suction with a vacuum pump.
  • a part of the clean gas discharged from the top of the adsorption tower during the adsorption operation is used as the purge gas, and the vacuum pump is operated so that the pressure in the adsorption tower becomes 100 to 300 Torr.
  • the purged exhaust gas containing gasoline vapor after desorption is mixed with the gasoline vapor-containing air generated from the exhaust gas generation source and then sent to the condenser, where it is partially liquefied and purged as liquid (gasoline liquid) Collect gasoline vapor in exhaust gas.
  • the present invention has been made to solve the above-described problems, and provides a small and inexpensive apparatus and method for treating and recovering gaseous hydrocarbons that can efficiently liquefy gasoline contained in gasoline vapor. It is intended.
  • a gaseous hydrocarbon treatment / recovery device is a gaseous hydrocarbon treatment / recovery device for treating / recovering gasoline vapor, comprising a condensing device for liquefying gasoline vapor, and the condensing device.
  • Gas-liquid separator that separates liquefied gasoline liquid and gasoline vapor
  • adsorption / desorption device that adsorbs / desorbs gasoline vapor separated by the gas-liquid separator
  • heat medium that cools the condensing device and the adsorption / desorption device
  • a heat medium storage tank that stores the heat medium supplied to the condenser and the adsorption / desorption device, and a refrigerator that cools the heat medium stored in the heat medium storage tank.
  • the method for treating and recovering gaseous hydrocarbons comprises sucking and pressurizing gasoline vapor, liquefying the gasoline vapor with a condensing device, and separating the gasoline liquid and gasoline vapor liquefied with the condensing device.
  • the heat medium is constantly supplied to the adsorption / desorption device, the heat cooled to the condensing device so that the gas temperature at the outlet of the condensing device becomes a predetermined temperature.
  • a medium is supplied.
  • the method for treating and recovering gaseous hydrocarbons comprises sucking and pressurizing gasoline vapor, liquefying the gasoline vapor with a condenser, and separating the gasoline liquid and gasoline vapor liquefied with the condenser.
  • the condensation device is cooled so that the pressure difference of the gasoline vapor at the inlet / outlet of the condensation device becomes a predetermined pressure. It is characterized in that a heated heat medium is supplied.
  • the heat medium can be supplied to each of the condensing device for liquefying gasoline vapor and the adsorption / desorption device for adsorbing and removing gasoline vapor.
  • the adsorption tower temperature can be made lower than the condensing device temperature while preventing moisture in the air from freezing and blocking the piping in the condensing device.
  • the gasoline vapor-containing air flowing in the condenser is cooled to a predetermined temperature above the freezing point. Steam can be liquefied efficiently.
  • FIG. 1 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to Embodiment 1.
  • FIG. 5 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to a second embodiment.
  • FIG. 6 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to Embodiment 3.
  • FIG. 6 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to a fourth embodiment.
  • FIG. 6 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to a fifth embodiment.
  • FIG. 10 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to a sixth embodiment.
  • FIG. 10 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to a seventh embodiment.
  • FIG. 9 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to an eighth embodiment.
  • FIG. 10 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to a ninth embodiment.
  • FIG. 10 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to Embodiment 10;
  • FIG. 1 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to Embodiment 1 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as gasoline vapor recovery device 100
  • This gasoline vapor recovery device 100 liquefies and recovers gasoline contained in gasoline vapor released into the atmosphere when gasoline is supplied.
  • the relationship of the size of each component may be different from the actual one.
  • the double line indicates the conduction of the heat medium
  • the normal solid line or the broken line indicates the conduction of the gasoline vapor-containing air
  • the thick solid line indicates the conduction of the gasoline liquid.
  • the gasoline vapor recovery device 100 includes an oil supply device 1, a gasoline vapor suction pump 2, a condenser tube 3, a heat medium storage tank 4, a heat exchanger 5, a refrigerator 6, an adsorption / desorption tower (adsorption / desorption tower). 7 and adsorption / desorption tower 8), gas-liquid separator 9, liquid circulation pump 10, suction pump 11, gasoline tank 12, pressure controller 13, gasoline vapor supply pipe 14, purified air discharge pipe 15, purge gas inlet pipe 16, purge gas discharge It has a pipe 17, a gas-liquid mixed gasoline outflow pipe 18, a temperature measuring device 19, and a condenser pipe cooling tank 20.
  • the gasoline vapor recovery device 100 includes a valve B1, a valve B2, a desorption valve B3, an adsorption discharge valve B4, a mass flow controller B5, an adsorption inflow valve B6, a heat medium supply control valve B7, a three-way valve (three-way valve C1). To C4).
  • the fueling device 1 has a fueling nozzle and the like, and has a function of fueling gasoline to automobiles such as passenger cars and motorcycles. In addition, the fueling device 1 functions as an inlet for sucking gasoline vapor that leaks during gasoline fueling.
  • the gasoline vapor suction pump 2 is connected to the refueling device 1 and the upstream side of the condensing pipe 3, and has a function of sucking gasoline vapor generated in the vicinity of the refueling portion of the refueling device 1 into the gasoline vapor recovery device 100. ing.
  • the condensing pipe 3 is disposed inside a condensing pipe cooling tank 20 to be described later, and is connected to the downstream side of the gasoline vapor suction pump 2 and the gas-liquid separator 9. It functions as a cooling pipe that liquefies.
  • the condensing tube cooling tank 20 functions as a heat medium container that cools the condensing tube 3 by disposing the condensing tube 3 therein and storing the heat medium supplied by the liquid circulation pump 10. That is, the condensing tube 3 and the condensing tube cooling tank 20 function as a condensing device for liquefying gasoline vapor.
  • the heat medium storage tank 4 is connected to the condensing tube cooling tank 20 and the liquid circulation pump 10 and stores a heat medium (for example, an antifreeze liquid composed of a petroleum-based substance such as propylene glycol, gasoline, kerosene). is there.
  • the heat exchanger 5 is provided in the heat medium storage tank 4 and has a function of cooling the heat medium stored in the heat medium storage tank 4 as one component of the refrigerator 6.
  • the refrigerator 6 is connected to the heat medium storage tank 4 through the heat exchanger 5 and is connected to a purge gas discharge pipe 17 between the gasoline vapor suction pump 2 and the suction pump 11 and uses a heat pump cycle. It has a function of supplying a refrigerant to the heat exchanger 5.
  • the connection state of the refrigerator 6 and the heat exchanger 5 is shown with the dashed-dotted line.
  • the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are configured so that the heat medium stored in the heat medium storage tank 4 and the gasoline vapor-containing air flowing out from the condensation pipe 3 circulate. It functions as a desorption device for desorption.
  • the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are filled with an adsorbent (for example, silica gel or zeolite) that adsorbs or removes (desorbs) gasoline vapor in the air containing gasoline vapor.
  • FIG. 1 shows an example in which the adsorption / desorption tower 7 operates as an adsorption tower and the adsorption / desorption tower 8 operates as a desorption tower.
  • the gas-liquid separator 9 is connected to the downstream side of the condensing pipe 3 and the adsorption / desorption tower 7 and the adsorption / desorption tower 8, and has a function of separating the gasoline liquid liquefied by the condensation pipe 3 and the gasoline vapor. Yes.
  • the gasoline liquid is guided to the gasoline tank 12, and the gasoline vapor is guided to the adsorption / desorption tower 7 and the adsorption / desorption tower 8.
  • the liquid circulation pump 10 is connected to the heat medium storage tank 4, and is connected to the condensing tube cooling tank 20, the adsorption / desorption tower 7, and the adsorption / desorption tower 8 via the three-way valve C 3, and is cooled by the heat exchanger 5.
  • the heated heat medium is supplied to the condenser tube cooling tank 20, the adsorption / desorption tower 7, and the adsorption / desorption tower 8.
  • the suction pump 11 is provided in the purge gas discharge pipe 17 between the adsorption / desorption tower 7 and the adsorption / desorption tower 8 and the refrigerator 6 and is adsorbed by the adsorbent filled in the adsorption / desorption tower 7 or the adsorption / desorption tower 8.
  • the gasoline tank 12 is connected to the gas-liquid separator 9 and the fueling device 1 and temporarily stores the gasoline liquid separated by the gas-liquid separator 9.
  • the pressure controller 13 is connected to the adsorption / desorption tower 7, the adsorption / desorption tower 8, and the purified air discharge pipe 15, and has a function of adjusting the pressure in the adsorption / desorption tower 7 and the adsorption / desorption tower 8.
  • the gasoline vapor feed pipe 14 is connected to the gas-liquid separator 9 and is branched in the middle to be connected to the adsorption / desorption tower 7 and the adsorption / desorption tower 8. It leads to the adsorption / desorption tower 7 or the adsorption / desorption tower 8.
  • the purified air discharge pipe 15 is connected to the pressure controller 13 and sends air discharged from the adsorption / desorption tower 7 and the adsorption / desorption tower 8 (clean gas including gasoline vapor of 1 vol% or less) to the atmosphere.
  • the purge gas inflow pipe 16 is connected to the purified air discharge pipe 15 and connects the adsorption / desorption tower 7 and the adsorption / desorption tower 8, and is discharged from the adsorption / desorption tower 7 or the adsorption / desorption tower 8 to the atmosphere. A part of the clean gas is sent as a purge gas to the adsorption / desorption tower 8 or the adsorption / desorption tower 7 for use.
  • the purge gas discharge pipe 17 is connected to the suction pump 11 and branched in the middle to be connected to the adsorption / desorption tower 7 and the adsorption / desorption tower 8, and was used for desorption in the adsorption / desorption tower 7 or the adsorption / desorption tower 8. The subsequent purge gas is conducted.
  • the gas-liquid mixed gasoline outflow pipe 18 is connected to the downstream side of the condensing pipe 3 and the gas-liquid separator 9 and conducts the gasoline liquid liquefied in the condensing pipe 3 and the gasoline vapor-containing air.
  • the temperature measuring device 19 is installed in the vicinity of the downstream side of the condensing tube 3, conducts the condensing tube 3, and measures the temperature of the gasoline vapor-containing air discharged from the condensing tube 3.
  • the temperature information measured by the temperature measuring device 19 is sent as a signal to a control device (not shown).
  • the valve B1 is connected to the fuel supply device 1 and is connected to a purge gas discharge pipe 17 between the gasoline vapor suction pump 2 and the refrigerator 6, and opens in conjunction with the operation of the fuel supply device 1. Yes.
  • the valve B ⁇ b> 2 is connected to the gas / liquid separator 9 and the gasoline tank 12, and is opened when the gasoline liquid collected by the gas / liquid separator 9 is supplied to the gasoline tank 12.
  • the detachment valve B3 is provided in each of the branched purge gas discharge pipes 17, and is opened when the purge gas is conducted by being controlled to open and close.
  • the desorption valve B3 provided in the purge gas discharge pipe 17 connected to the adsorption / desorption tower 7 will be referred to as a desorption valve B3 '.
  • the adsorption discharge valve B4 is provided in each of the pipes connecting the adsorption / desorption tower 7 and the adsorption / desorption tower 8 and the pressure controller 13, and is controlled to be opened and closed so that the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are provided.
  • the gasoline vapor-containing air that has been adsorbed by the gas is conducted.
  • the adsorption discharge valve B4 provided in the pipe connected to the adsorption / desorption tower 8 will be referred to as an adsorption discharge valve B4 '.
  • the mass flow controller B5 is provided in each of the purge gas inflow pipes 16 with the purified air discharge pipe 15 interposed therebetween, and controls the gas amount of the purge gas by being controlled to open and close.
  • the mass flow controller B5 provided in the purge gas inflow pipe 16 connected to the adsorption / desorption tower 7 will be referred to as a mass flow controller B5 '.
  • the adsorption inflow valve B6 is provided in each of the branched gasoline vapor supply pipes 14, and leads the gasoline vapor-containing air to the adsorption / desorption tower 7 or the adsorption / desorption tower 8 by being controlled to open and close.
  • the adsorption inflow valve B6 provided in the gasoline vapor supply pipe 14 connected to the adsorption / desorption tower 8 will be referred to as an adsorption inflow valve B6 '.
  • the heat medium supply control valve B7 is provided between the liquid circulation pump 10 and the condensing pipe cooling tank 20, and is controlled by opening and closing to control the heat medium supplied from the heat medium storage tank 4 to the condensing pipe cooling tank 20. The amount is adjusted.
  • the three-way valve C1 is connected to the condensing pipe cooling tank 20, the heat medium storage tank 4, and the three-way valve C2, and changes the distribution destination of the heat medium by switching control.
  • the three-way valve C2 is connected to the adsorption / desorption tower 7, the adsorption / desorption tower 8, and the three-way valve C1, and changes the flow destination of the heat medium by switching control.
  • the three-way valve C3 is connected to the condensing pipe cooling tank 20, the liquid circulation pump 10, and the three-way valve C4, and changes the flow destination of the heat medium by switching control.
  • the three-way valve C4 is connected to the adsorption / desorption tower 7, the adsorption / desorption tower 8, and the three-way valve C3, and changes the flow destination of the heat medium by switching control. It is assumed that a control device (not shown) executes the opening / closing of each valve, the switching of the flow path of each three-way valve, the control of the refrigerator 6 and the like.
  • the operation of the gasoline vapor recovery device 100 will be described.
  • the valve B1 is opened in conjunction with it, and the gasoline vapor suction pump 2 is operated.
  • gasoline vapor (about 40 vol% at normal temperature) in the vicinity of the refueling part of the refueling device 1 is sucked into the gasoline vapor recovery device 100 and added to, for example, about 0.2 to 0.4 MPa.
  • the air is sent to the condensation tube 3.
  • the condensation pipe 3 is provided in the condensation pipe cooling tank 20 and is cooled by a heat medium stored in the condensation pipe cooling tank 20. Usually, the inside of the condensing tube cooling tank 20 is maintained at about 0 ° C.
  • the gasoline vapor concentration is about 10 vol%.
  • the saturated gasoline vapor concentration is about 10 vol% at a pressure of 0.3 MPa and a temperature of 5 ° C.
  • the gasoline vapor concentration should theoretically be 10 vol% or less. There is no. Further, the gasoline vapor concentration at the outlet of the condenser tube 3 can be reduced by lowering the temperature.
  • the setting temperature of the condensing tube 3 is about 0 to 5 ° C. It is desirable to make it.
  • the valve B2 is opened.
  • the gasoline liquid accumulated in the lower part of the gas-liquid separator 9 is returned to the fuel supply device 1 via the gasoline tank 12.
  • the valve B2 is closed, and the gasoline liquid is stored again in the lower part of the gas-liquid separator 9.
  • the gasoline tank 12 since the gasoline tank 12 is provided, the gasoline vapor is prevented from flowing into the gas-liquid separator 9, and the adsorption / desorption tower 7 and the adsorption / desorption tower 7 due to the high concentration gasoline vapor flowing into the adsorption / desorption tower 8 and Shortening the adsorption breakthrough time of the adsorption / desorption tower 8 (shortening the switching timing) is prevented.
  • the gasoline tank 12 has a structure in which gasoline vapor is present in the upper part. For this reason, even when the valve B2 is opened, the gasoline vapor does not flow into the gas-liquid separator 9 due to the flow of the gasoline liquid, and the high-concentration gasoline vapor does not enter the adsorption / desorption tower 7 or the adsorption / desorption tower 8. Can be prevented from being insufflated.
  • FIG. 1 shows a case where the adsorption / desorption tower 7 operates as an adsorption tower and the adsorption / desorption tower 8 operates as a desorption tower. Therefore, the detaching valve B3 is open (black), the detaching valve B3 ′ is closed (white), the suction discharge valve B4 is open (black), and the suction discharge valve B4 ′ is closed (black). The suction inflow valve B6 is open (black), and the suction inflow valve B6 ′ is closed (white).
  • the detachment valve B3 is closed, the detachment valve B3 ′ is opened, the adsorption discharge valve B4 is closed, the adsorption discharge valve B4 ′ is opened, the adsorption inflow valve B6 is closed, and the adsorption inflow valve B6 'is used as open.
  • the desorption of gasoline in the adsorption / desorption tower 7 is completed, it is used again as an adsorption tower, and this operation is repeated over time.
  • Switching between adsorption and desorption is performed by switching between the desorption valve B3 and desorption valve B3 ′, the adsorption discharge valve B4 and the adsorption discharge valve B4 ′, the adsorption inflow valve B6 and the adsorption inflow valve B6 ′ as described above. To control.
  • the gasoline vapor is supplied to the adsorption / desorption tower 7 through the gasoline vapor supply pipe 14.
  • An adsorbent that adsorbs gasoline vapor is enclosed in the adsorption / desorption tower 7 and the adsorption / desorption tower 8.
  • silica gel particularly silica gel having a pore size of 4 to 100 angstrom or synthetic zeolite alone or a mixture thereof is effective.
  • the gasoline components are adsorbed and removed, and become clean air having a gasoline concentration of 1 vol% or less and released to the atmosphere through the purified air discharge pipe 15.
  • the purified air discharge pipe 15 is provided with a pressure controller 13 for controlling the pressure of the clean air discharged to the atmosphere to a specified value, and this pressure controller 13 is adsorbed when discharging the clean air to the atmosphere.
  • the pressure in the adsorption / desorption tower 7 operating as a tower is maintained at a specified value.
  • the gasoline vapor is adsorbed by using the high-pressure (about 0.3 MPa) exhaust gas of the condensing pipe 3, so that it is more adsorbed than at normal pressure. Adsorption capacity is greatly improved.
  • the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are always cooled to a constant temperature by a heat medium supplied by the liquid circulation pump 10 regardless of the role of gasoline vapor adsorption / desorption. That is, the operation of the cooling system of the condenser tube 3, the adsorption / desorption tower 7 and the adsorption / desorption tower 8 is always controlled so as to be maintained at the set temperature. This is because the adsorbent filled in the adsorption / desorption tower 7 and the adsorption / desorption tower 8 is cooled by heat transfer from the fin tube heat exchanger provided in the adsorption / desorption tower 7 and the adsorption / desorption tower 8. This is because a certain amount of cooling time is indispensable and it cannot cope with instantaneous operation.
  • the provision of the refrigerator 6 having a large cooling capacity so that it can be cooled in a short time adversely affects the equipment cost, making it impossible to provide an inexpensive gasoline vapor recovery device.
  • the adsorption capacity of the adsorbent can be increased, and the amount of adsorbent used can be reduced.
  • the temperature of the adsorbent in the adsorption / desorption tower 7 and the adsorption / desorption tower 8 rises when the gasoline vapor recovery is stopped, the gasoline vapor is desorbed from the adsorbent filled in the adsorption / desorption tower 7 and the adsorption / desorption tower 8.
  • the pressure in the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be prevented from rising.
  • the gasoline vapor desorption process When desorbing gasoline adsorbed by the adsorbent packed in the adsorption / desorption tower 8 operating as the desorption tower, the gas is discharged from the adsorption / desorption tower 8 via the purge gas discharge pipe 17 by driving the suction pump 11. To desorb gasoline from the adsorbent. At this time, the demounting valve is opened (black), and the demounting valve B3 ′ is closed (white).
  • the adsorption / desorption tower that functions as an adsorption tower at the time of adsorption is operating at a high pressure of 0.3 MPa. However, the adsorption pump 11 is depressurized to the atmospheric pressure or less by the suction pump 11 at the time of desorption. Gasoline is desorbed.
  • the desorbed gasoline vapor is returned to the condensing pipe 3 in FIG. 1, and after the gasoline is condensed and recovered again, it is returned to the adsorption / desorption tower 7 again. While this operation is repeated, the entire amount of gasoline is condensed and recovered in the condensing pipe 3.
  • the desorption speed can be increased by increasing the temperature inside the adsorption / desorption tower 8.
  • energy consumption increases in the heating means such as the refrigerator 6 and the heater. Since there is a problem that the adsorption / desorption tower 7 and the adsorption / desorption tower 8 cannot be switched in a short time, it is effective to perform desorption at the same temperature as during adsorption without increasing the temperature during desorption.
  • the efficiency is not so high only by the desorption method using the pressure difference due to the suction of the suction pump 11, it is effective to introduce the purge gas from the outside. Therefore, in the first embodiment, a part of the clean gas discharged from the adsorption / desorption tower 7 to the atmosphere as the purge gas is sent to the adsorption / desorption tower 8 by the purge gas inflow pipe 16 and used.
  • the gas flow rate of the purge gas is controlled by the mass flow controller B5 and the mass flow controller B5 '.
  • the mass flow controller B5 is opened (blacked out) so that a specified amount of gas can be circulated, and the mass flow controller B5 'is closed (outlined) so that no gas flows.
  • the amount of moisture in the gas is sufficiently reduced in the pre-stage condensing tube 3, so that the moisture contained in the purge gas has little adverse effect on the adsorbent in the adsorption / desorption tower 8. .
  • the desorption test it was found that when the purge gas flow rate was 15 to 25 L / min, the pressure in the adsorption tower could be 15 to 30 kPa, and gasoline vapor could be desorbed efficiently.
  • the set temperature of the heat medium stored in the condensing tube cooling tank 20 is 0 ° C. to 5 ° C. in order to prevent water contained in the gas from freezing in the condensing tube 3. It is desirable to set the temperature to about ° C.
  • the temperature of the adsorbent is as low as possible (for example, below freezing point). Therefore, it is considered that by setting the cooling temperatures of the condensing tube 3, the adsorption / desorption tower 7 and the adsorption / desorption tower 8 to different temperatures, it is possible to recover gasoline more efficiently than in the past.
  • the condensation tube 3 and the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be controlled to different temperatures, so that it is possible to efficiently recover gasoline.
  • the three-way valve C1 to the three-way valve C4 as the flow path switching means, it is possible to make the supply amount of the heat medium different between the condensation pipe 3, the adsorption / desorption tower 7, and the adsorption / desorption tower 8. It has become.
  • the heat medium storage tank 4 is provided with a heat exchanger 5, and the heat medium is stored so that the heat exchanger 5 is sufficiently immersed.
  • the refrigerator 6 When the refrigerator 6 is operated, the heat medium in the heat medium storage tank 4 is cooled to a predetermined temperature via the heat exchanger 5. At that time, the temperature of the heat medium is measured, and the operation of the refrigerator 6 may be controlled by the signal.
  • the heat medium cooled to a predetermined temperature is supplied to the adsorption / desorption tower 7 and the adsorption / desorption tower 8 by the liquid circulation pump 10.
  • the heat medium supplied to the adsorption / desorption tower 7 and the adsorption / desorption tower 8 is cooled back to the adsorption / desorption tower 7 and the adsorption / desorption tower 8 and then returned to the heat medium storage tank 4 again.
  • the adsorbent in the adsorption / desorption tower 7 and the adsorption / desorption tower 8 is cooled to a predetermined temperature.
  • the heat medium is always supplied to the adsorption / desorption tower 7 and the adsorption / desorption tower 8 having a large heat capacity regardless of the operation of the oil supply apparatus 1 and the role of gasoline vapor adsorption / desorption. It has become. Thereby, it is possible to sufficiently cope with intermittent load inflow, and to realize a highly reliable gasoline vapor recovery apparatus 100.
  • the cooling temperature of the adsorbent is preferably as low as possible based on the adsorption characteristics, and in order to realize this, the cooling temperature of the heat medium is preferably as low as possible.
  • the cooling temperature of the adsorbent is desirably set to ⁇ 20 ° C. to 0 ° C. From the above, by setting the cooling temperature of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 to ⁇ 20 ° C. to 0 ° C., the adsorption efficiency of the adsorbent can be increased, and the gasoline is liquefied efficiently and compactly.
  • a gasoline vapor recovery device 100 that can condense can be obtained.
  • the heat medium cooled to a predetermined temperature is supplied by the liquid circulation pump 10 to the condensing tube cooling tank 20 via the heat medium supply control valve B7.
  • the heat medium stored in the condensation pipe cooling tank 20 and the heat medium supplied from the heat medium storage tank 4 are mixed.
  • the heat medium deprives the heat generated from the condensation tube 3 and is returned to the heat medium storage tank 4 again.
  • the temperature measuring device 19 measures the temperature of the outlet gas of the condensing tube 3
  • the heat medium supply control valve B 7 is opened and closed so that the temperature does not fall below the freezing point, and the heat medium supplied to the condensing tube cooling tank 20. The amount is controlled.
  • the gasoline vapor-containing air flowing in the condenser 3 is cooled to a predetermined temperature above the freezing point.
  • gasoline vapor can be efficiently liquefied without freezing moisture in the gas.
  • the heat medium cooled by the liquid circulation pump 10 is always supplied to the adsorption / desorption tower 7 and the adsorption / desorption tower 8, but the condensation pipe cooling tank 20 is operated by the oil supply device 1.
  • a heat medium is supplied by the liquid circulation pump 10. That is, since the condensing tube 3 is made of metal, heat conduction is fast and it can be cooled relatively quickly, so that the gas temperature at the outlet of the condensing tube 3 reaches a predetermined value in accordance with the operation of the fueling device 1.
  • the heat medium is supplied by the liquid circulation pump 10.
  • the case where the amount of the heat medium supplied to the condensing tube cooling tank 20 is on / off controlled by opening and closing the heat medium supply control valve B7 is shown as an example.
  • the flow rate may be controlled.
  • the temperature of the heat medium in the condensing tube cooling tank 20 can be controlled to a higher degree. From the above, by setting the cooling temperature of the condensing tube 3 to a temperature above the freezing point, it is possible to prevent the formation of icing in the condensing tube 3, and the gasoline vapor that can recover gasoline with high reliability and efficiency.
  • the recovery device 100 can be obtained.
  • the fueling device 1 stops when the fueling is completed.
  • the controller B5 and the suction inflow valve B6 are fully closed.
  • the heat medium is always supplied to the adsorption / desorption tower 7 and the adsorption / desorption tower 8 and the adsorbent is cooled, the gasoline vapor is desorbed and the adsorption / desorption tower 7 and the adsorption / desorption tower.
  • the pressure in 8 does not increase.
  • the desorption valve B3 and the desorption valve B3 ′ provided at the lower part of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are opened, and the gasoline vapor adsorbed at the lower part of the adsorption / desorption tower 7 is absorbed.
  • the pressure rise of the adsorption / desorption tower 7 and the pressure of the adsorption / desorption tower 8 may be made equal to alleviate the pressure rise.
  • the gas temperature at the outlet of the condensing tube 3 is measured by the temperature measuring device 19 and the amount of the heat medium supplied to the condensing tube cooling tank 20 is controlled.
  • the pressure difference of the gasoline vapor at the inlet / outlet of the condensing tube 3 may be measured by the differential pressure gauge 21 and the amount of the heat medium supplied to the condensing tube cooling tank 20 may be controlled.
  • the supply amount of the heat medium may be controlled so that the pressure difference measured by the differential pressure gauge 21 becomes a predetermined pressure.
  • the gas temperature at the outlet of the condensing tube 3 is measured by the temperature measuring device 19 and the amount of the heat medium supplied to the condensing tube cooling tank 20 is controlled.
  • the temperature of the heat medium may be measured by the temperature measuring device 19 at the portion where the heat medium is supplied.
  • the gas temperature in the condensing tube 3 is measured. Temperature control that achieves almost the same performance can be realized. However, since the temperature measurement is performed at a location where heat media with different temperatures are mixed, it is necessary to measure the temperature of the heat medium while the temperature of the heat medium fluctuates relatively violently, and the heat medium reaches the set temperature. It is difficult to judge that the gas temperature in the condensing tube 3 is measured, and it is inferior to the gas temperature measuring method in the condensing tube 3.
  • FIG. FIG. 2 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 2 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as a gasoline vapor recovery device 200
  • This gasoline vapor recovery apparatus 200 liquefies and recovers gasoline contained in the gasoline vapor released into the atmosphere when gasoline is supplied, as in the gasoline vapor recovery apparatus according to the first embodiment.
  • differences from the first embodiment will be mainly described, and the same parts as those in the first embodiment will be denoted by the same reference numerals and description thereof will be omitted.
  • the gas temperature at the outlet of the condenser tube 3 is measured by the temperature measuring device 19 and the amount of the heat medium supplied to the condenser tube cooling tank 20 is controlled as an example.
  • the pressure difference between the inlet and the outlet of the condensing tube 3 is measured using the differential pressure gauge 21, and the value is compared with the set value so as to control the amount of the heat medium supplied to the condensing tube cooling tank 20.
  • This differential pressure gauge 21 measures the pressure difference of gasoline vapor at the inlet and outlet of the condenser tube 3 from the pressure of gasoline vapor at the inlet side of the condenser tube 3 and the pressure of gasoline vapor at the outlet side of the condenser tube 3. is there.
  • the pressure difference information measured by the differential pressure gauge 21 is sent as a signal to a control device (not shown).
  • the gasoline vapor recovery apparatus 200 provides a gasoline vapor recovery apparatus 200 that can control the amount of the heat medium supplied to the condensing tube cooling tank 20 with higher accuracy and can liquefy and recover gasoline with high efficiency. can do.
  • FIG. 3 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 3 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as a gasoline vapor recovery device 300
  • This gasoline vapor recovery device 300 liquefies and recovers gasoline contained in the gasoline vapor released into the atmosphere during gasoline refueling, similar to the gasoline vapor recovery device according to the first and second embodiments. is there.
  • differences from the first and second embodiments will be mainly described, and the same parts as those in the first and second embodiments will be denoted by the same reference numerals and the description thereof will be omitted. It shall be.
  • the condensing pipe 3 is provided in the condensing pipe cooling bath 20
  • a pipe connecting the liquid separator 9 and the condenser tube 3 to the gas-liquid separator 9 is provided inside the second heat medium cooling tank 31 which is a heat medium container, and the cooled heat medium is supplied to the second heat medium cooling tank 31.
  • the gas-liquid separator 9 and the pipe connecting the condenser tube 3 and the gas-liquid separator 9 the gasoline liquid liquefied in the condenser tube 3 reaches the gas-liquid separator 9.
  • the condenser tube 3 and the second heat medium cooling tank 31 function as a condensing device for liquefying gasoline vapor.
  • the gasoline vapor can be efficiently recovered, the gasoline vapor removed by the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be reduced, and the adsorbent to be used can be reduced.
  • the energy-saving and compact gasoline vapor recovery apparatus 300 can be provided.
  • the temperature measuring device 19 is installed in the gasoline vapor recovery apparatus 300 is shown as an example, a differential pressure gauge 21 similar to that of the second embodiment is used instead of the temperature measuring device 19 or temperature measurement. You may make it install with the container 19.
  • FIG. 4 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 4 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as a gasoline vapor recovery device 400
  • This gasoline vapor recovery device 400 liquefies and recovers gasoline contained in the gasoline vapor released into the atmosphere during gasoline refueling, similar to the gasoline vapor recovery device according to the first to third embodiments. is there.
  • differences from the first to third embodiments will be mainly described. The same parts as those in the first to third embodiments are denoted by the same reference numerals, and the description thereof is omitted. It shall be.
  • the heat medium used for cooling the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be directly supplied to the condenser tube cooling tank 20. That is, after the heat medium is supplied to the adsorption / desorption tower 7 and the adsorption / desorption tower 8 by the liquid circulation pump 10, the heat medium returns directly to the heat medium storage tank 4 via the heat medium return valve B8, and the heat medium supply control valve. The case where it supplies directly to the condensation pipe cooling tank 20 via B7 can be controlled.
  • the heat medium return valve B8 is connected to the heat medium supply control valve B7, the three-way valve C1, and the three-way valve C2, and the three-way valve C5 and the three-way valve C1 provided between the three-way valve C1 and the three-way valve C2. It is provided between.
  • the temperature of the heat medium supplied to the condensing tube cooling tank 20 can be increased by the heat generated in the adsorption / desorption tower 7, and the heat medium and the condensing pipe originally present in the condensing tube cooling tank 20. Since the temperature difference of the heat medium supplied to the cooling tank 20 can be reduced, the gas temperature inside the condenser tube 3 can be controlled with higher accuracy. Therefore, it is possible to provide the gasoline vapor recovery apparatus 400 that can liquefy gasoline with high efficiency.
  • a differential pressure gauge 21 similar to that of the second embodiment is used instead of the temperature measuring device 19 or temperature measurement. You may make it install with the container 19.
  • FIG. FIG. 5 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 5 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as gasoline vapor recovery device 500
  • This gasoline vapor recovery device 500 liquefies and recovers gasoline contained in the gasoline vapor released into the atmosphere when gasoline is supplied, like the gasoline vapor recovery device according to the first to fourth embodiments. is there.
  • differences from the first to fourth embodiments will be mainly described, and the same parts as those in the first to fourth embodiments will be denoted by the same reference numerals and the description thereof will be omitted. It shall be.
  • the fifth embodiment is different from the fourth embodiment in that a temperature controller 41 is provided between the heat medium supply control valve B7 and the condenser tube cooling tank 20.
  • the temperature of the heat medium supplied to the condensing tube cooling tank 20 can be made higher than the temperature of the heat medium discharged from the outlets of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 by the temperature controller 41, and the condensation pipe Since the temperature difference between the heat medium originally present in the cooling tank 20 and the heat medium supplied to the condensing pipe cooling tank 20 can be reduced, the gas temperature inside the condensing pipe 3 can be controlled with higher accuracy. From the above, it is possible to provide the gasoline vapor recovery apparatus 500 that can liquefy gasoline with high efficiency.
  • FIG. 6 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 6 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as gasoline vapor recovery device 600
  • This gasoline vapor recovery device 600 is a device that liquefies and recovers gasoline contained in gasoline vapor released into the atmosphere during gasoline refueling, similar to the gasoline vapor recovery device according to the first to fifth embodiments. is there.
  • differences from the first to fifth embodiments will be mainly described, and the same parts as those in the first to fifth embodiments will be denoted by the same reference numerals and the description thereof will be omitted. It shall be.
  • the condensing pipe 3 and the condensing pipe cooling tank 20 are changed to a condensing heat exchanger 52 and a condensing container 51 for storing the condensing heat exchanger 52.
  • This is different from Form 5. That is, the condensing heat exchanger 52 and the condensing container 51 serve as a condensing device for liquefying gasoline vapor.
  • the condensation heat exchanger 52 it is most suitable to use a finned tube heat exchanger in that the pressure loss is small and the gas containing gasoline vapor can be efficiently cooled.
  • the type of the condensing container 51 is not particularly limited as long as the condensing container 51 can store the condensing heat exchanger 52 therein.
  • the operation of the gasoline vapor recovery device 600 will be briefly described.
  • the gasoline vapor suction pump 2 starts operating along with the operation of the fueling device 1
  • the gasoline vapor is sucked and supplied to the condensing container 51 that stores the heat exchanger 52 for condensation.
  • the gasoline vapor sent to the condensing container 51 flows through the condensing container 51 and is liquefied on the surface of the condensing heat exchanger 52.
  • a heat medium is supplied to the condensing heat exchanger 52 by the liquid circulation pump 10 via a heat medium supply control valve B7.
  • the gasoline vapor sent to the condensing container 51 is cooled by this heat medium.
  • the gas temperature at the outlet of the condensing container 51 is measured by the temperature measuring device 19, and the heat medium supply control valve B7 is opened and closed to control the amount of heat medium supplied to the heat exchanger for condensation 52.
  • the heat medium supply control valve B7 is opened and closed to control the amount of heat medium supplied to the heat exchanger for condensation 52.
  • the temperature measuring device 19 is installed in the gasoline vapor recovery apparatus 600 is shown as an example, a differential pressure gauge 21 similar to that of the second embodiment is used instead of the temperature measuring device 19 or temperature measurement. You may make it install with the container 19.
  • a heat medium return valve B8 similar to that of the fourth embodiment may be provided.
  • FIG. 7 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 7 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as a gasoline vapor recovery device 700
  • This gasoline vapor recovery device 700 liquefies and recovers gasoline contained in the gasoline vapor released into the atmosphere during gasoline refueling, similar to the gasoline vapor recovery device according to the first to sixth embodiments. is there.
  • differences from the first to sixth embodiments will be mainly described, and the same parts as those in the first to sixth embodiments will be denoted by the same reference numerals and the description thereof will be omitted. It shall be.
  • the seventh embodiment is different from the sixth embodiment in that a metal particle 53 is placed in a condensing container 51 provided with a heat exchanger 52 for condensation.
  • a metal particle 53 aluminum, copper, or the like, which has good heat conduction and is not corroded by gasoline vapor or the like, is suitable. By doing in this way, since a gasoline vapor
  • the structure of the condensing container 51 can be made the same as that of the adsorption / desorption tower 7 and the adsorption / desorption tower 8. be able to.
  • a gasoline vapor recovery apparatus 700 that can liquefy gasoline at low cost and with high efficiency.
  • a differential pressure gauge 21 similar to that of the second embodiment is used instead of the temperature measuring device 19 or temperature measurement. You may make it install with the container 19.
  • a heat medium return valve B8 similar to that of the fourth embodiment may be provided.
  • the metal particles 53 may be made of a material that has good heat conduction and is not corroded by gasoline vapor or the like, and is not limited to aluminum or copper.
  • FIG. 8 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 8 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as gasoline vapor recovery device 800
  • This gasoline vapor recovery device 800 liquefies and recovers gasoline contained in the gasoline vapor released into the atmosphere during gasoline refueling, similar to the gasoline vapor recovery device according to the first to seventh embodiments. is there.
  • differences from the first to seventh embodiments are mainly described, and the same parts as those in the first to seventh embodiments are denoted by the same reference numerals and the description thereof is omitted. It shall be.
  • the gas temperature at the outlet of the condenser tube 3 is measured by the temperature measuring device 19 (or the differential pressure gauge 21) while always supplying a heat medium to the adsorption / desorption tower 7 and the adsorption / desorption tower 8.
  • the amount of the heat medium supplied to the condenser tube cooling tank 20 is controlled, but in the present embodiment 8, the second heat medium supply control valve is also used for the adsorption / desorption tower 7 and the adsorption / desorption tower 8.
  • the heat medium is always supplied only to the adsorption / desorption tower 7 that operates as an adsorption tower, and it operates as a desorption tower.
  • the supply amount of the heat medium is limited to the adsorption / desorption tower 8.
  • the second heat medium supply control valve B9 is provided in a pipe between the three-way valve C4 and the adsorption / desorption tower 7, and the third heat medium supply control valve B10 is provided in a pipe between the three-way valve C4 and the adsorption / desorption tower 8. ing.
  • the temperature of the adsorption / desorption tower 8 operating as the desorption tower can be increased, and the gasoline vapor can be efficiently desorbed from the adsorption / desorption tower 8. Therefore, the roles of the adsorption / desorption tower 7 and the adsorption / desorption tower 8. When the is switched, it can be sufficiently adsorbed.
  • the temperature of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be controlled, and the gasoline vapor recovery apparatus 800 capable of liquefying and recovering gasoline with high efficiency can be provided because the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are compact.
  • the case where the number of condensing parts is one (condensation tube 3 and condensing tube cooling tank 20) and the number of adsorption / desorption towers is two (absorption / desorption tower 7 and adsorption / desorption tower 8) is supplied to each.
  • the amount of the heat medium supplied to the plurality of condensing units and the plurality of adsorption / desorption towers is controlled by the same method. It may be. By doing in this way, the temperature of a some condensing part and a some adsorption / desorption tower can be controlled separately, and gasoline can be liquefied efficiently.
  • the temperature measuring device 19 is installed in the gasoline vapor recovery apparatus 800 is shown as an example, a differential pressure gauge 21 similar to that of the second embodiment is used instead of the temperature measuring device 19 or temperature measurement. You may make it install with the container 19.
  • a heat medium return valve B8 similar to that of the fourth embodiment may be provided.
  • the heat exchanger 52 for condensation instead of the condensation pipe
  • the condensation container 51 may be filled with the metal particles 53.
  • FIG. 9 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 9 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as gasoline vapor recovery device 900
  • This gasoline vapor recovery device 900 liquefies and recovers gasoline contained in the gasoline vapor released into the atmosphere during gasoline refueling, similar to the gasoline vapor recovery device according to the first to eighth embodiments. is there.
  • differences from the first to eighth embodiments will be mainly described, and the same parts as those in the first to eighth embodiments will be denoted by the same reference numerals and description thereof will be omitted. It shall be.
  • the second pressure controller 61 is disposed at the gas outlet of the gas-liquid separator 9 so that only the pressure inside the condensing pipe 3 is increased. Is different. Since the second pressure controller 61 is disposed at the gas outlet of the gas-liquid separator 9, the pressure inside the condensing tube 3 can be set higher. As a result, the gasoline vapor concentration at the outlet of the condenser tube 3 can be further lowered, and the gasoline concentration supplied to the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be lowered. Therefore, the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be reduced. Note that the pressure inside the gas-liquid separator 9 can also be increased by the second pressure controller 61.
  • the condensing pipe 3 is a spirally wound pipe, it is not necessary to handle it as a pressure vessel, and the pressure can be increased.
  • the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are pressure vessels, when the pressure is increased, it is necessary to have a pressure-resistant structure, and the vessel cost increases. Therefore, the apparatus can be made inexpensive by increasing the pressure of only the condensing tube 3 and setting the internal pressure of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 to 0.3 MPa or less which is not handled as a pressure vessel. From the above, it is possible to provide a gasoline vapor recovery apparatus 900 that can liquefy gasoline with low cost, compactness, and high efficiency.
  • the second pressure controller 61 which is a pressure control valve, is provided at the subsequent stage of the gas-liquid separator 9, whereby the pressure inside the condensing tube 3 as the condensing apparatus and the gas-liquid separator 9 Since the internal pressure can be increased, the saturated evaporation concentration of organic hydrocarbons such as butane and pentane, which have a high boiling point and are difficult to liquefy, can be lowered. It can be liquefied efficiently and the efficiency of gasoline vapor recovery will be improved.
  • the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are kept at a predetermined pressure or less by keeping the pressures of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 whose adsorption amount does not increase as the pressure increases. It is not necessary to set the pressure resistance of 8 too high, and the cost can be reduced.
  • the temperature measuring device 19 is installed in the gasoline vapor recovery apparatus 900 is shown as an example, a differential pressure gauge 21 similar to that of the second embodiment is used instead of the temperature measuring device 19 or temperature measurement. You may make it install with the container 19.
  • a heat medium return valve B8 similar to that of the fourth embodiment may be provided.
  • the heat exchanger 52 for condensation instead of the condensation pipe
  • the condensation container 51 may be filled with the metal particles 53.
  • FIG. FIG. 10 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 10 of the present invention.
  • a gaseous hydrocarbon treatment / recovery device hereinafter simply referred to as gasoline vapor recovery device 1000
  • This gasoline vapor recovery device 1000 liquefies and recovers gasoline contained in the gasoline vapor released into the atmosphere during gasoline refueling, similar to the gasoline vapor recovery device according to the first to ninth embodiments. is there.
  • differences from the first to ninth embodiments will be mainly described, and the same parts as those in the first to ninth embodiments will be denoted by the same reference numerals and the description thereof will be omitted. It shall be.
  • the integrated flow meter 71 is provided in the purified air discharge pipe 15 for sending the air discharged from the adsorption / desorption tower 7 or the adsorption / desorption tower 8 to the atmosphere. 9 and different. Thereby, the integrated quantity of the gas discharged
  • the capacities of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are reduced to the maximum, the entire apparatus is made compact, the switching time between the adsorption / desorption tower 7 and the adsorption / desorption tower 8 is lengthened, and the life of the valve is lengthened. There is an effect that the life of the apparatus can be extended.
  • the integrated flow meter 71 is provided in the purified air discharge pipe 15 connected to the outlets of the adsorption / desorption tower 7 and the adsorption / desorption tower 8, the adsorption / desorption tower 7 and the adsorption / desorption tower The total amount of air that has passed through 8 can be clearly seen, and the function of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 is reversed without an expensive gasoline concentration meter, that is, switching between the adsorption tower and the desorption tower. The timing can be clarified. In addition, the capacity of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be reduced to the maximum so that the entire apparatus can be made compact.
  • a differential pressure gauge 21 similar to that of the second embodiment is used instead of the temperature measuring device 19 or temperature measurement. You may make it install with the container 19.
  • a heat medium return valve B8 similar to that of the fourth embodiment may be provided.
  • the heat exchanger 52 for condensation instead of the condensation pipe
  • the condensation container 51 may be filled with the metal particles 53.
  • a second pressure controller 61 similar to that of the ninth embodiment may be provided.

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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

La présente invention concerne un appareil de traitement/récupération d’hydrocarbure gazeux non onéreux et compact, capable d’efficacement liquéfier l’essence contenue dans la vapeur d'essence ; et un procédé associé. La présente invention décrit un appareil de récupération de vapeur d’essence (100) caractérisé par le fait qu’il comprend un tube de condensation (3) destiné à liquéfier la vapeur d’essence ; un séparateur gaz-liquide (9) destiné à séparer la vapeur d’essence de l’essence liquide ayant été liquéfiée par le tube de condensation (3), fourni postérieurement au et sur le côté aval du gaz du tube de condensation (3) ; des colonnes d’adsorption désorption (colonne d’adsorption désorption (7) et colonne d’adsorption désorption (8)) pour l’adsorption désorption de la vapeur d’essence ayant été séparée par le séparateur gaz-liquide (9), fournies postérieurement au et sur le côté aval du gaz du séparateur gaz-liquide (9) ; une cuve de piégeage de milieu chaud (4) destinée à stocker un milieu chaud adaptée au stockage du milieu chaud pour refroidir le tube de condensation (3) et les colonnes d’adsorption désorption et pour fournir le milieu chaud à une cuve de refroidissement de tube de condensation (20) et aux colonnes d’adsorption désorption ; et un réfrigérateur (6) destiné à refroidir le milieu chaud stocké dans la cuve de piégeage de milieu chaud (4).
PCT/JP2008/056007 2008-03-28 2008-03-28 Appareil et procédé de traitement/récupération d’hydrocarbure gazeux WO2009118876A1 (fr)

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PCT/JP2008/056007 WO2009118876A1 (fr) 2008-03-28 2008-03-28 Appareil et procédé de traitement/récupération d’hydrocarbure gazeux
JP2010505103A JP5289427B2 (ja) 2008-03-28 2008-03-28 ガス状炭化水素の処理・回収装置及び方法
CN200880128078.4A CN101970082B (zh) 2008-03-28 2008-03-28 气状碳氢化合物的处理回收装置以及方法
KR1020107019909A KR101215211B1 (ko) 2008-03-28 2008-03-28 가스상태 탄화 수소의 처리· 회수 장치 및 방법
TW097115218A TW200940156A (en) 2008-03-28 2008-04-25 Gaseous hydrocarbon treating/recovering apparatus and method

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JP5693448B2 (ja) * 2009-03-31 2015-04-01 三菱電機株式会社 ガス状炭化水素の回収装置及び方法
CN109200745A (zh) * 2018-08-31 2019-01-15 江苏新久扬环保设备科技有限公司 一种油气吸附回收装置及工艺
CN113457569A (zh) * 2021-07-28 2021-10-01 湖北兴瑞硅材料有限公司 适用于二甲基二氯硅烷水解物裂解的真空装置及工艺

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CN103349885B (zh) * 2013-07-23 2015-04-15 蔡兵 油蒸汽回收系统及回收方法
KR20170109187A (ko) * 2016-03-18 2017-09-28 삼성디스플레이 주식회사 휘발성 유기화합물 제거 장치 및 휘발성 유기화합물 제거 방법
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CN110068488A (zh) * 2019-03-27 2019-07-30 北京航空航天大学 一种无损采集固定源烟气中半挥发性有机物的装置及方法

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TW200940156A (en) 2009-10-01
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