TW201034741A - Apparatus and method for recovering gaseous hydrocarbon - Google Patents

Abstract

A small and inexpensive apparatus for recovering a gaseous hydrocarbon is provided which can efficiently liquefy the gasoline contained in gasoline vapor. Also provided is a method of recovering a gaseous hydrocarbon. The gasoline vapor recovery apparatus (100) comprises: a condensation tube (3) which cools gasoline vapor; a gas-liquid separator (9) which separates the gasoline liquid which has been condensed and liquefied by cooling with the condensation tube (3) from the gasoline vapor remaining unliquefied; an adsorption/desorption column in which the gasoline vapor separated by the gas-liquid separator (9) is adsorbed and desorbed; and a second condensation tube (20) to which the gasoline vapor desorbed in the adsorption/desorption column is supplied and which cools this gasoline vapor.

Description

201034741 22~second heat medium storage tank; 23~second pressure controller; 1 〇〇~/-L oil vapor recovery device; Bl, Β2~ valve; Β3, Β3'~ separation valve; Β4, Β4, 〜 Discharge valve for adsorption; Β5, Β5, ~ mass flow controller Β6, Β6' Β7~ valve. ~Adsorption inflow valve; When the five cases have a chemical formula on the right, please reveal the best indication of the characteristics of the invention. Sub-5^ · Sixth, invention description: [Technical field to which the invention pertains] ° The invention relates to a recovery device and method for gas-like hydrocarbons to be contained in an atmosphere-releasing gas, in particular, for treating and recovering gasoline A device and method for vaporizing gasoline vapor that leaks during oil supply. π [Prior Art] A gas generated by an exhaust gas generating source (containing about 4 〇ν〇% of a gasoline vapor exhaust gas) in a gas-like hydrocarbon recovery apparatus and method using a conventional adsorbent separating agent The air is supplied from the exhaust gas supply pipe to the condensate by the pressure of the fan or itself, and the liquefied gasoline vapor is partially liquefied in the condensate 3 3 201034741, and the unliquefied gasoline vapor is supplied to the adsorption tower to complete the adsorption process. The treated exhaust gas is discharged into the atmosphere from the top of the adsorption tower (the adsorption tower after switching to the separation process) via the discharge pipe via air (clean air) containing lv〇1% or less of gasoline vapor. Then, in the adsorption tower after completion of the adsorption process, the exhaust gas is sent through the exhaust gas supply pipe, and is suctioned by the vacuum pump to be separated. A part of the cleaning device discharged from the top of the adsorption tower during the adsorption operation is used as a gas for exhaust gas, and the pressure in the adsorption tower is 100 to 300 T rr to operate the vacuum pump. After the separation, the exhaust gas is mixed with the air containing the π oil therapy π generated by the exhaust gas generation source, and then sent to the condenser, and the liquid is liquefied in the condenser to be used as a liquid (gasoline liquid) to recover the exhaust gas. Gasoline vapor in the gas. With such a configuration, 'gasoline vapor can recover substantially all of the vapor of the liquid, thus the gas-like hydrocarbon recovery device and method in this configuration: 'discharge from the adsorption tower # gasoline vapor concentration is low enough, and π causes The degree of large-scale dyeing (for example, refer to Patent Document g 1). In the technique of Patent Document 1, the moisture of the φ preparation w and the second emulsion is mixed into the first condensing device, and when the cooling temperature is below the freezing point, the water freezes in the first condensing device, and the first condensation is blocked. Device. m .1 ^ Therefore, the cooling temperature of the first condensing unit must be set above the freezing point. Patent Document 1: JP-A-2006-1 98604 (pages 4 to 8, page 2 and page 9 to page 10 of Figure 6) [Summary of the Invention] 4 201034741 [Problems to be solved by the invention] However, At this set temperature, the low-boiling hydrocarbon such as butane and isobutylene, which are the main components of the gasoline vapor, does not liquefy, and flows into the adsorption tower in this state, and the time during which the gasoline vapor leaks from the adsorption tower is shortened, and the time for the adsorption tower to switch is also reduced. Will be shortened. Further, the switching time of the adsorption tower is not shortened, and the adsorption tower becomes large, that is, the amount of the adsorbent charged in the adsorption tower must be increased or even increased. In addition, in the method of condensing the gasoline vapor sucked from the nozzle of the oil supply and the gasoline vapor separated from the adsorption tower and condensing in the condensing device, the gasoline and the vapor of the gasoline having a low relative concentration of the gas are sucked from the nozzle. It is mixed with concentrated gasoline vapor separated by a tower. Therefore, the concentration of low-boiling hydrocarbons such as butane and isobutane having a high saturated vapor pressure concentration is also low in the gas, and is not condensed in the condensation tower, but is again supplied to the adsorption tower, not only low-boiling hydrocarbons. Poor recovery rates will also waste energy. In order to solve the above problems, the present invention provides a hydrocarbon recovery apparatus and method for efficiently liquefying gasoline contained in gasoline steam. [Means for Solving the Problem] The gas-like hydrocarbon recovery device of the present invention comprises: a condensing device for cooling > fly oil steam; a gas-liquid separator, which is provided on the downstream side of the condensing device, and is condensed and liquefied by cooling in the condensing device The gasoline liquid is separated from the unliquefied alpha oil vapor; an adsorption separation device is disposed on the downstream side of the gas-liquid separation gas to suck the gasoline vapor separated by the gas-liquid separator, and a second condensation device is connected In the above adsorption separation device, the gasoline vapor adsorbed and separated by the adsorption separation device is supplied thereto to cool the gasoline vapor of 5 201034741. The gas-like hydrocarbon recovery device of the present invention comprises: a deformable gas supply device for changing a gas flow rate of the gasoline vapor to be sucked; and a condensing device for cooling the gasoline vapor supplied from the deformable gas supply device; a gas-liquid separator, which is disposed on a downstream side of the condensing device, is separated from the unliquefied gasoline vapor by the condensing device, and is condensed and liquefied; and an adsorption separation device is disposed on the downstream side of the gas of the gas-liquid separator The gasoline vapor separated by the gas-liquid separator is adsorbed and separated. The gas-like hydrocarbon recovery device of the present invention comprises: a condensing & 'cooling gasoline vapor; a gas-liquid separator 'located on the downstream side of the condensing device', and condensing and liquefying the gasoline liquid and unliquefied in the condensing device a gasoline vapor separation; a refrigeration device disposed on a downstream side of the gas of the gas-liquid separator to cool the gasoline vapor separated from the gas-liquid separator; and an adsorption separation device disposed on a downstream side of the refrigeration device The gasoline vapor cooled by the above refrigeration device is adsorbed and separated. The gas-like hydrocarbon recovery device of the present invention comprises: a condensed through-cooled gasoline vapor; a gas-liquid separator disposed on a downstream side of the condensing device, and condensed and liquefied in the condensing device to be liquefied and unliquefied a gasoline vapor separation; a compression pump to pressurize and compress the gasoline vapor flowing out from the gas-liquid separator; and a second condenser disposed on the downstream side of the gas of the gas-liquid separator to be cooled and separated by the gas-liquid separator The compressed gasoline vapor is pressurized by the above compression pump. The gas-like hydrocarbon recovery device of the present invention comprises: _condensing through-cooled gasoline vapor; and a gas-liquid separator disposed downstream of 201034741 of the condensing device::! The gasoline liquid which is cooled and condensed and liquefied by the condensing device is separated from the unliquefied gasoline; the downstream side of the milk body is adsorbed and separated, and the gasoline separated by the gas-liquid separator is distilled and separated; And a second adsorption separation device that adsorbs and separates gasoline vapor which is muscled from the adsorption separation device. In the method for recovering gaseous hydrocarbons according to the present invention, the gas-like hydrocarbon recovery device described above is used to condense the adsorbed and separated condensed gasoline containing concentrated gasoline vapor at a time when oil is not supplied, and during the period of oil supply, The air containing the attracted gasoline vapor is treated by mixing with air containing adsorbed separated concentrated gasoline vapor. In the method for recovering gaseous hydrocarbons of the present invention, the above-described gas-like hydrocarbon recovery device is used to switch the adsorption device and the separation device of the adsorption separation device in a predetermined period of time. [Effects of the Invention] According to the gas-like hydrocarbon recovery device of the present invention, since the second condensing device for condensing the gasoline vapor separated from the adsorption separation device is provided, the gasoline vapor separated from the adsorption separation device can be separately condensed. Therefore, the gasoline vapor having a relatively low relative concentration sucked from the nozzle is mixed with the concentrated gasoline vapor separated from the adsorptive separation device to prevent a decrease in concentration in a gas having a low vapor boiling point of hydrocarbon such as butane or isobutane having a high saturated vapor pressure concentration. It can efficiently condense and recover low boiling point hydrocarbons. According to the gas-like hydrocarbon recovery device of the present invention, the gas flow rate of the air containing the gasoline vapor is changed by providing the deformable gas supply device. The low-boiling hydrocarbon can be efficiently adsorbed by the adsorption separation device, and is filled in the adsorption separation device of 7 201034741. The amount of adsorbent used is reduced. Therefore, an inexpensive and compact gas-like hydrocarbon recovery device can be obtained. According to the gas-like hydrocarbon recovery device of the present invention, the refrigerant is vaporized by the gas-liquid separator on the downstream side of the gas-liquid separator, and the gasoline vapor is contained in the adsorption separation device. The temperature of the air can be made lower. Therefore, the ability to remove low boiling hydrocarbons in the adsorptive separation apparatus can be increased. According to the gas-like hydrocarbon recovery device of the present invention, by providing a compression pump for pressurizing and compressing the gasoline vapor flowing out of the gas-liquid separator, the gasoline vapor can be compressed in two stages, and the butane having a low boiling point and being difficult to be liquefied can be reduced. And the saturated evaporation concentration of organic hydrocarbons such as isobutylene can be effectively liquefied in the second cold-extinguishing device to improve the recovery efficiency of gasoline vapor. According to the gas-like hydrocarbon recovery device of the present invention, by providing the second adsorption separation device for low-boiling hydrocarbon, the adsorption separation device and the second adsorption separation device can separately separate and regenerate the gasoline component, and can be efficiently recovered. The separated low boiling point hydrocarbon contained in the concentrated gasoline. According to the gas-like hydrocarbon recovery method of the present invention, since the functions of the adsorption device and the separation device in the adsorptive separation device are appropriately switched, the recovery efficiency of the gasoline vapor can be improved. [Embodiment] Hereinafter, embodiments of the present invention will be described based on the drawings. Embodiment 1 FIG. 1 is a schematic view showing a structure of a gasoline circuit of a first embodiment of the present invention. The figure f 2 is a schematic configuration diagram of another structure of the gasoline vapor recovery device 100. According to Fig. 1 and Fig. 2, a gasoline vapor recovery device 1 as a gas-like hydrocarbon recovery device will be described. . The circuit structure and the flow of gasoline vapor. Further, in the first drawing, in the following drawings, the relationship of the dimensions of the respective members is different from the actual elements. The A-oil vapor recovery device 1 is installed at a gas station together with an oil supply device 1 that supplies gasoline to a car or the like. The gasoline vapor recovery unit i

Ο From the oil supply. The gasoline vapor sucked in the vicinity of the crucible is cooled and recovered by the condenser 3, and two adsorption separation devices (adsorption knife away from the tank) for adsorbing or separating the gasoline vapor are provided. Switching to recover (adsorb) and reuse (separate) gasoline vapor. The gasoline vapor recovery device 1 has a gasoline vapor suction pump 2, a condensation tube 3, a heat medium storage tank 4, a heat exchanger 5, a cold money 6, two suction, and a liquid circulation pump attachment separation tower (adsorption separation tower 7, 8) gas-liquid separator 10, suction pump 11, gasoline tank 12, pressure controller 13, gasoline steam feed pipe 14, purified air discharge pipe 15, exhaust gas inflow pipe 16, exhaust gas discharge f 17, gas The liquid mixed gasoline outflow pipe 18, the gasoline vapor compression pump 19, the second condensation pipe 2G, the second gas-liquid separator 21, the second heat medium storage tank 22, and the second pressure controller 23. The gasoline vapor is drawn into the gasoline vapor recovery unit 100 via a nozzle of the 纟® st. The condenser 3 cools the inhaled gasoline vapor and condenses and liquefies. In the heat medium storage tank 4, while the condenser 3 is housed inside, it stores brine for cooling the condenser 3. The heat exchanger 5 constitutes a freezer 6: 9 201034741 'cooling the heat medium reservoir' and while the refrigerant is being wounded, the heat medium accommodated in the heat medium storage tank 4 is stored in the heat sink. Cold; the east machine 6 is provided with a cold reel to the heat exchanger 5 constituting the cold; east coil. ~^(four) tower? The 8 series is filled with an adsorbent that removes the gasoline vapor contained in the condensing pipe 3 and removes the gasoline vapor in the work disorder (for example, the boiling (four) bub (four) is the function of the adsorption tower for adsorbing the gasoline vapor and serves as the separated gasoline vapor. The function of the separation column. In the figure i, the adsorption knife is operated from the column 7 as an adsorption column (hereinafter referred to as adsorption $7), and

The adsorption separation column 8 is shown as an example of the operation of the separation column (hereinafter referred to as separation ¥ 8). The gas-liquid separator 9 is connected to the downstream side of the condenser 3, and the gasoline liquid liquefied in the condenser 3 is separated from the gasoline vapor by gas-liquid separation. The liquid circulation pump 10 is connected to the heat medium storage tank 4 and the two adsorption separation columns, and supplies the heat medium cooled by the heat exchanger 5 to the adsorption separation columns 7, 8. The attracting fruit 11 is provided in a pipe connecting the two adsorption separation columns for sucking and separating the gasoline vapor adsorbed by the adsorbents in the adsorption separation columns 7, 8. The gasoline tank I is connected to the gas-liquid separator 9 and the oil supply device 1, and the gasoline liquid separated by the gas-liquid separator 9 is temporarily stored. The pressure controller 13 is provided in the purified air discharge pipe 15 connected to the two adsorption separation columns, and has a function of adjusting the pressure in the two adsorption separation columns. The gasoline vapor supply pipe 14 is connected to the gas-liquid separator 9 and the two adsorption separation columns as a conduit for introducing the gasoline vapor separated from the gas-liquid separator 9 into the adsorption separation column. The purified air discharge pipe 15 is connected to two adsorption separation columns, which are pipes for discharging the gasoline vapor and discharging the air discharged from the adsorption separation tower to the atmosphere. The exhaust gas flow human pipe 16 is connected to the two adsorption separation towers, and is used as the adsorption separation tower 7 or the adsorption separation tower 8 to transport the waste gas of the clean gas discharged to the atmosphere as an exhaust gas to be transported to the adsorption separation tower. 7 or the piping of the adsorption separation column 8. The exhaust gas discharge pipe 17 is connected to the suction pump u and two

吸附 Adsorption separation column The separation row of the adsorption separation column 7 or the adsorption separation column 8 = the pipe in which the emulsion is conducted to the second heat medium storage tank 22. Gas-liquid mixed gasoline Steaming = the outflow pipe 18 is a pipe connecting the condensation f 3 and the gas-liquid separator 9. The vapor-vapor compression system 19 is disposed between the suction pump and the second heat medium storage tank 22 to compress the concentrated gasoline vapor discharged from the suction pump. The second condenser pipe 20 is connected to the exhaust gas discharge pipe π for condensing the π oil component in the air containing the concentrated gasoline vapor compressed by the gasoline vapor compression pump 9 . The second gas-liquid separator 21 is connected to the downstream side of the second condenser pipe 20, which is an element for gas-liquid separation of the gasoline liquid liquefied in the second condenser pipe 2 and the steam vapor. The second heat medium storage tank 22 stores a heat medium such as brine for cooling the second condenser 2 contained therein. The second pressure controller 23 is connected to the second gas-liquid separator 21, and the pressure of the second condenser 2 is adjusted by adjusting the pressure in the second gas-liquid separator 21, and is in the gasoline vapor recovery device 100. The valve B1 disposed between the oil supply device 1 and the black alpha suction fruit 2, and the valve B2 disposed between the gas-liquid separator 9 and the gasoline tank 12 are disposed in the two adsorption separation towers and the suction pump 11 The separation pipe B3, the adsorption discharge pipe B4 provided between the two adsorption separation columns and the pressure controller 13, and the mass flow rate of the exhaust gas 11 201034741 body inlet pipe 16 provided to the two adsorption separation columns The controller B5 includes an adsorption inflow valve B6 provided in the middle of the gasoline vapor supply pipe 14 of the two adsorption separation columns, and a valve B7 provided between the second gas-liquid separator 21 and the gasoline tank 12. Moreover, the open valve is shown in black and the blocked valve is shown in reverse (added in the symbol). The valve B1 is interlocked with the operation of the oil supply device. The valves are opened when the gasoline liquid recovered by the gas-liquid separator 9 is supplied to the gasoline tank 12. The separation valve B3 is opened when the separated exhaust gas of the adsorption separation column 7 or the adsorption separation column 8 is turned on. The adsorption discharge valve B4 is used to adjust two adsorption separation columns: pressure: opening and closing. The mass flow controller B 5 is used to adjust the amount of gas flowing through the exhaust gas inflow pipe 16 to open and close. The adsorption inflow valve (4) is opened when the gasoline vapor is supplied from the gas-liquid separator 9. The intermediate B7 is opened when the gasoline liquid recovered by the second orifice liquid knife separator 21 is supplied to the gasoline tank 12.

Pair > flying oil vapor recovery unit

When the oil supply device 1 is actuated, the valve B1 is opened and the gasoline vapor pump is started. So, in the vicinity of the oil supply part of the oil supply unit 4, the steam is sucked into the gasoline vapor recovery device by steam (normal temperature Xiao 4 () ν 〇 1%), for example, pressurized and deflated to 〇·2~〇· 4 MPa. The air supply to the condenser condenser 3 is disposed in the heat medium storage tank 4 and is cooled by a heat medium stored in the heat medium reservoir 4. Intercooling. Therefore, in the case of the cold shirt 3, the inside of the condensing camp is usually stored in the condensing camp. The internal part of the condensing camp is stored at ~5 ° C, and the moisture contained in the gasoline and gas is partially condensed. Then, 'flow into the gas-liquid separator 9, from this, the operation of the condensing pipe 3, oil vapor" and liquid (gasoline). The condition is pressure 〇.3 MPa, cooling temperature 5 ° c, 12 201034741 gas flow rate 100 L/min'. Under this condition, when the gasoline vapor recovery device is operated, the concentration of gasoline vapor supplied to the condensing pipe 3 is 1 〇ν〇1%. Moreover, from the saturation concentration diagram of gasoline vapor (not shown), the saturated gasoline vapor concentration at pressure of 0.3 MPa and temperature | 5 t is about 10% by volume. Under this condition, the gasoline vapor concentration is theoretically not Below ι〇ν〇ι%. Further, by lowering the temperature, the gasoline vapor concentration at the outlet of the condenser 3 can be reduced. Therefore, when the set temperature is below the freezing point, the enthalpy contained in the gas

The water freezes in the condensing pipe 3, and the set temperature of the condensing pipe is preferably Ot~ due to the problem of #配#blocking. Also, when the oil supply time reaches a predetermined time, % β2 is open. Thereby, the gasoline liquid remaining in the lower portion of the gas-liquid separator 9 is returned to the oil supply device 1 via the gasoline tank 12. Thereafter, after a predetermined period of time, the valve B2 is closed, and the gasoline liquid is again accumulated in the lower portion of the gas-liquid separator 9. Thus, since the gasoline tank 12 is provided, it is possible to prevent the gasoline vapor from flowing into the gas-liquid separator 9. Thus, it is possible to prevent the absorption time of the adsorption knife from the column 7 or the adsorption separation column 8 from being shortened due to the concentration of the gasoline vapor flowing to the separation column 7 or the adsorption separation column 8 (shortening of the switching order). As shown in the figure '1', in the gasoline tank 12, a certain amount is accumulated in the lower portion. - The gasoline liquid separated by the liquid helium emulsion separator 9 flows in from the bottom, and flows downward from the bottom in the steam: 2. By this, it becomes a structure in which gasoline is present in the gasoline tank. Therefore, when the valve cartridge 2 is opened, the gasoline & gas does not flow into the gas-liquid separator 9 due to the flow of the gasoline liquid, and the oil vapor is not supplied to the adsorption separation column 7 or the adsorption separation column 8. X π is treated in a large WGvq 1% gasoline vapor system 13 201034741 which cannot be treated by the condenser 3 to the adsorption separation column 7 or the adsorption separation column 8 (the adsorption separation column 7 as the adsorption extraction in Fig. 1). Therefore, at this time, the separation room B3 becomes. When it is opened (blackened), the separation valve β3 is turned into a closed state, and the suction discharge valve Β4 is opened (blackened) by the suction, and the suction valve 64 is closed, and (reverse) is closed.斛用&人Μ# The slave catching valve Β6 is opened (blackened), and the suction inflow valve Β6' (reverse white) is in a locked state. After the adsorption column 7 is adsorbed at any time, it is used as a separation column. At this time, the separation port 3, the adsorption discharge valve β4, and the adsorption inflow port 6 are closed, and D/f is separated, the blade valve β3, the adsorption discharge valve 64, and the adsorption inflow valve Β6'. Also a, ^ ^ ° becomes an open state. Further, when the separation is completed, it is again used as an adsorption tower, and #m causes the operation to be used repeatedly in time. The switching of the adsorption and separation is performed by the above-described switching between the scalpel valve B3 and the separation valve B3, the adsorption discharge valve B4, the adsorption discharge valve, and the adsorption inflow valve B6 and the adsorption inflow valve. And control. Therefore, in the condensing pipe 3, the gasoline vapor is processed and sent to the adsorption tower 7 through the gasoline steam supply pipe. Right In the adsorptive separation column 7 and the adsorptive separation column 8, as described above, the adsorbent having an adsorption vapor /lw of 4 is sealed. The adsorbent for adsorbing vapor vapor, particularly a tantalum or a synthetic zeolite having a pore diameter of 4 to iU0 angstrom, is effective. The oil vapor is passed through the adsorbent, and the gasoline vapor component is removed and removed by the adsorbent, and the clean air having a gasoline concentration of 1 v ο 1 % or less is discharged to the atmosphere via the clean annual air-drying discharge pipe 15 . . In addition, in the clean air discharge pipe 15 which discharges the clean air to the big friend's milk, as described above, the pressure control is arranged to cry, and the sputum separation tower 7 14 201034741 and the adsorption separation tower 8 The pressure is controlled at the specified value. In the first embodiment, the adsorption capacity of the high pressure (about 〇3 MPa) of the condensing pipe 3 is used, and the adsorption capacity is greatly improved by adsorption under normal pressure. The adsorption separation column 7 and the adsorption separation column 8 are independent of the effect of adsorption separation of the gasoline vapor, and the heat medium supplied from the liquid circulation pump 1 经常 is often cooled to a predetermined temperature. That is, the cooling system of the condenser 3 and the two adsorption separation columns is often controlled to operate at a predetermined set temperature. The adsorbent charged in the adsorptive separation column 70 and the adsorptive separation column 8 is cooled by heat transfer by the fin-and-tube heat exchanger provided in the adsorptive separation column 7 and the adsorptive separation column 8, and a certain degree of cold time is necessary. Indispensable, it cannot correspond to the instantaneous operation. Further, the refrigerator 6 having a large cooling capacity which is cooled in a short period of time has an adverse effect on the equipment cost, and it is impossible to provide an inexpensive gasoline recovery device. Further, by lowering the temperature in the adsorption tower 7, the adsorption capacity of the adsorbent becomes large, and the amount of the adsorbent used can be reduced. Further, since the adsorption separation column 7 and the adsorption separation column 8 are maintained at a predetermined set temperature, and the gasoline vapor recovery is stopped, the gasoline vapor is separated from the adsorption due to the temperature rise of the adsorbent in the adsorption separation column 7 and the adsorption separation column 8. The separation of the adsorbent in the column 7 and the adsorption separation column 8 can effectively prevent the pressure in the adsorption separation column 7 and the adsorption separation column 8 from rising. Explain the separation process of gasoline vapor. When the gasoline adsorbed to the adsorbent is separated, the suction pump 11 draws gas from the separation column 8 via the exhaust gas discharge pipe 17, and the gasoline is separated from the adsorbent. At this time, the separation valve B3 is opened, and the separation valve B3 is closed. Although the adsorption tower (in this case, the adsorption tower 7) is operated at the adsorption state of 3 MPa in the high pressure state 15 201034741 state, the adsorption pressure is caused to be adsorbed to the adsorbent by the pressure difference from the suction pump 11 to the atmospheric pressure or lower during the separation. The separation of gasoline. The separated gasoline vapor is compressed by the gasoline vapor compression pump 19 and the second pressure controller 23, and is sent to the second condenser 20. The second condenser tube 20 is disposed in the second heat medium storage tank 22 and is cooled by a heat medium stored in the second heat medium storage tank 22. Therefore, the gasoline vapor is cooled while the second condenser 2 is turned on. Usually, the inside of the second condensing duct 20 is kept at a temperature of 〇 ° C to 5 ° C. The moisture contained in the gasoline and the gas partially condenses. Thereafter, it flows into the second gas-liquid separator 21, and is separated into gas and liquid (gasoline, water) by the second gas-liquid separator 21. When the gasoline in the second gas-liquid separator 21 reaches a predetermined amount, the valve b7 is opened. Thereby, the gasoline liquid accumulated in the lower portion of the second gas-liquid separator 21 is returned to the oil supply device 1 via the gasoline tank 12. On the other hand, about 1 〇v〇l% of the gasoline vapor which cannot be processed in the second condenser 2〇 is returned to the adsorption tower 7 via the second pressure controller 23 and the gasoline vapor supply pipe 14. In other words, the "steamed gasoline vapor" taken from the separation column 8 is maintained at a high concentration and supplied to the second condensation & 20, and is effectively liquefied, and the unliquefied gasoline vapor is again adsorbed and removed in the adsorption tower 7. At the time of separation, by the method of suctioning the pressure difference caused by the suction of the pump U, since the separation efficiency is not so high, the exhaust gas is efficiently introduced from the outside. Here, a part of the clean gas discharged from the adsorption tower 7 to the atmosphere as the exhaust gas is supplied to the separation column 8 by the exhaust gas inflow pipe 16. The mass flow controller β5 and the mass flow controller B5' control the flow rate of the gas passing through the exhaust gas inflow pipe 16. At this time, the quality of the 201034741 flow controller B5 is in an open state, and the mass flow controller B5 is in a locked state. That is, the mass flow controller B5 passes the predetermined amount of the gas 'mass flow controller B5 in the open state, and is in the locked state without passing through the gas. Further, in the first embodiment, in the front-stage condenser 3, since the amount of moisture in the gas is sufficiently low, the moisture contained in the exhaust gas does not adversely affect the adsorbent in the separation column 8.

切换 The switching of the adsorptive separation column 7 and the adsorptive separation column 8 will be described. As described above, the gasoline vapor is adsorbed and removed by the adsorption tower 7 to form a clean air having a gasoline concentration of lv 〇 1% or less, and is discharged to the atmosphere via the purge air discharge pipe 15 . Therefore, supply to the adsorption tower? The amount of steam vapor increases, and the adsorption capacity of the adsorption tower 7 gradually decreases. This state is continued, and when the concentration of the gasoline at the outlet of the adsorption tower 7 is close to 1%, the adsorption separation column 7 and the adsorption separation column 8 must be switched. In the oil sump, the oil supply system is not regularly performed. Therefore, when the adsorption separation column 7 is switched between the adsorption separation column 8 and the adsorption separation column 8 in a simple manner, the adsorption operation of the adsorption separation column 7 and the adsorption separation may be caused by the oil supply tank. So, you, , and , 丄 #, left ... ~ 1% by the strip steam recovery device (10), and the switch from the tower 7 and the adsorption separation tower 8 to the gasoline recovery unit 1 〇n female The integral value of the time when the Η just started is effectively entered. That is, when the integral value of the η* oil recovery device and the operation time reaches a predetermined time, the adsorption separation column 7盥' and the separation column 8 are switched, and the integral value is set again from the tongue. Into, ° Ding action time integral calculation. Further, the indicator indicating that the gasoline vapor recovery device 100 is actuated is the operation of the gasoline 201034741 steam suction "2" and the attraction system 11. In the gasoline vapor recovery device 100, since the gasoline vapor suction pump 2 is synchronized with the suction pump ,, there is no problem in the operation time of one of the integral calculations. Further, the timing of the actual switching: Even if the integral calculation time reaches a predetermined value, it is not necessary to switch immediately but to switch after a predetermined time. The cooling control method of the second condenser 20 will be described. The heat medium in the heat medium storage tank 4 cooled by the cold machine 6 is supplied from the liquid circulation pump 10 to the second heat medium storage #22 by the second tube 2. It is cooled. Further, in the figure, the piping supplied to the separation tower two media is diverged, and although the heat medium is supplied to the second heat medium storage tank 22', it is not limited thereto. That is, the supply of the heat medium to the second heat medium storage tank 22, the adsorption separation column 7, and the adsorption separation column 8 may be performed side by side. Therefore, the supply of the heat medium to the second heat medium storage tank 22 may be different from the piping through which the heat medium supplied to the adsorption tower 7 flows, and the outlet of the liquid circulation may be divided into three directions. The reason why the supply of the heat medium to the second heat medium storage tank 22, the adsorption separation column 7, and the adsorption separation column 8 is performed side by side is that the heat medium is directed to the second heat medium storage tank 22, the adsorption separation column 7, and the adsorption separation column 8 In the case of the column, the temperature of the heat medium in the last flowing machine (the machine located at the most downstream) is higher than the predetermined temperature. Therefore, the performance of the machine is lowered, and the performance of the entire gasoline vapor recovery device 100 is lowered. The manner in which the separated gasoline vapor is separately condensed as a feature of the gasoline vapor recovery of the first embodiment is compared with a conventional method. The separated gasoline vapor is separately condensed by mixing the gasoline vapor separated in the adsorption separation column 18 201034741 with the gasoline vapor taken in from the oil supply unit, and separately condensing separately (hereinafter referred to as the present mode). Moreover, the conventional method of comparison is the separation of the gasoline tomb steam disk m flyfield... the gasoline vapors taken by the several oil supply devices are mixed and condensed. The figure 9 shows the gasoline composition (horizontal axis) and each of the prior art. A diagram of the amount of machine (vertical axis). Fig. 3 is a graph showing the relationship between the gasoline component (horizontal axis) corresponding to the length of the oil supply time and the amount of each machine (vertical axis) in the technique. Fig. 11 is a graph showing the saturation concentration of the saturated concentration of the gasoline component at 〇3MPa (the horizontal axis is the temperature pc) and the vertical axis is the saturated concentration [v〇1%]. Fig. 12 is a graph showing the saturation concentration of the saturated concentration of the π oil component (the pressure is [MPa] on the horizontal axis and the saturation concentration [v〇1%] on the vertical axis). According to the ninth to nth diagrams, the recovery of the low boiling point hydrocarbons will be described with reference to the composition of π'. In Fig. 9, four elements of the gasoline vapor recovery unit ( (gasoline tank 12 (a), gasoline vapor compression pump 19 (b), gas-liquid separator 9 outlet (c), adsorption separation tower The amount of gasoline component exported (d)). In the Fig. 9, the amount of the gasoline component at the time of supplying 250 L of oil is shown. From Fig. 9, the amount of low boiling point hydrocarbons (C4 hydrocarbon and C5 hydrocarbon) is not reduced in the gas-liquid separator 9. Further, the amount of the outlet of the adsorption separation column of the low boiling point hydrocarbon in Fig. 9 is not reduced. In Fig. 10, it shows the amount (f) of the n* oil component at the outlet of the adsorption separation column at 50 L of oil supply and the amount (f) of the gasoline component at the outlet of the adsorption separation column at 285 L of oil supply. From the i-th diagram, as the oil supply time increases, the leakage of low-boiling hydrocarbons (especially C4 hydrocarbons such as butane and isobutane and C5 hydrocarbons burned at the far end and isoprene 19 201034741) Increase. From Fig. 9 and the figure, although the recovery efficiency of low-boiling hydrocarbons is improved, the recovery efficiency of the entire gasoline vapor is also improved. From Fig. 11, the recovery efficiency of the gasoline vapor is increased by using low temperature. This principle is also in the form of the present invention, and it is also known in the art that the cooling medium is used to cool the heat medium in the heat medium storage tank and to maintain the adsorption separation column at a predetermined temperature. From Fig. 12, the saturated concentration of gasoline vapor, particularly the saturated concentration of low boiling hydrocarbons, is affected by the pressure. From Fig. 11 and Fig. 12, the recovery efficiency of low-boiling hydrocarbons is increased by low temperature and pressure (described in the sixth embodiment for the two-stage compression). The concentration of isobutane in the gasoline-containing air taken in from the oil supply device was 40 vol%, the gas flow rate was 7 〇L/min, and the isobutane concentration in the separated air containing gasoline vapor was 70 〇1. %, the gas flow rate is 30 L / min, compared with the conventional method and the present mode. Further, the condensation conditions were a gas pressure of MPa·3 MPa and a cooling temperature of 2°C. The saturated vapor concentration of isobutyl burn under this condition was 56 vol%. Therefore, in the conventional mode, the concentration of isobutane containing gasoline vapor at the time of mixing is 49 v 〇 I%, which is below the saturated vapor concentration. Under such conditions, isobutane could not be recovered in its entirety. On the other hand, in the aspect of the present invention, isobutane containing gasoline vapor from the oil supply device cannot be recovered, and the butane in the separated gasoline-containing air can be recovered 4.2 L/min [3〇L/min χ (7〇ν〇ι% a 56v〇1%)]. In this manner, the amount of low boiling point hydrocarbons such as butadiene and isobutylene flowing into the adsorption tower is reduced, and the load on the adsorption tower is reduced, so that the adsorption tower can be downsized and the adsorption separation timing can be extended. Therefore, 20 201034741 By the gasoline vapor recovery apparatus 100, the low boiling point hydrocarbon such as butane and isobutane can be recovered by the means of the present invention, and a gasoline recovery apparatus 100 which is compact and can efficiently liquefy the condensed gasoline vapor can be obtained. As described above, the gasoline recovery unit f1 of the first embodiment is provided with a condensing device (second condensing pipe 20) for condensing air containing separated concentrated gasoline vapor, and contains the condensing device from the oil supply device. Since the air of the gasoline vapor is a condensing device (condensation pipe 3) for condensing, it is possible to efficiently recover low-boiling hydrocarbons such as butadiene and isobutylene which cannot be recovered in a conventional manner. In addition, the gasoline vapor recovery device 100 can efficiently recover low-boiling hydrocarbons without a decrease in the condensing temperature and an increase in the compression pressure, and can operate the cold beam machine 6 in a state where the cooling efficiency is high. Further, since the gasoline vapor recovery device 100 reduces the power of the gasoline vapor compression pump 19, it does not consume unnecessary energy, and energy can be efficiently and efficiently recovered. In addition, the gasoline vapor recovery device 100 can reduce the amount of adsorbent used by effectively liquefying low-boiling hydrocarbons, thereby achieving miniaturization of the adsorption tower. Further, in the first embodiment, the pressure of the piping between the gasoline vapor compression pump 19 and the second pressure controller 23 is set to be different from that of the adsorption separation tower 7 by the second pressure controller 23. The pressure controller 13 in the rear stage of the tower 8 has the same value, but if the same value is to be set, the same effect can be obtained without setting the first pressure controller 23. However, the air from the fuel supply device 1 has a second condensing pipe 2 that does not have to flow into the condensed separation gas. Further, when the second force controller 23 is provided, the set pressure of the pressure controller 23 is higher than the set pressure of the pressure controller 13 by 21 201034741. By this, it is possible to efficiently recover the low-point hydrogen carbide contained in the concentrated gasoline vapor. Further, in the first embodiment, the second heat medium storage tank 22 is provided, and the heat medium is supplied to the second heat medium storage tank 22 by the liquid circulation pump 1 to cool the second condenser 20, but As shown in Fig. 2, a heat medium storage tank 31 for simultaneously cooling the condenser 3 and the second condenser 2 can be provided, and a procedure for circulating the heat medium can be performed in the adsorption separation columns 7, 8, thereby reducing At the same time as the number of components, the capacity of the liquid circulation pump 1 可 can be reduced. Therefore, the gasoline vapor recovery device 1 can reduce the amount of heat generated by the liquid circulation pump 10, and becomes an inexpensive and low-energy device. (Embodiment 2) Fig. 3 is a schematic structural view showing the entire structure of a gasoline vapor recovery device 1a in accordance with a second embodiment of the present invention. According to Fig. 3, the structure of the gasoline vapor recovery unit 100 a and the flow of gasoline vapor will be described. The gasoline vapor recovery device 10A is the same as the gasoline vapor recovery device 100 of the first embodiment. 'The gasoline vapor is cooled and recovered in the condenser pipe 3, and the functions of the two adsorption separation columns for adsorbing or separating the gasoline vapor are appropriately switched. A device that recovers (adsorbs) and reuses (separates). In the second embodiment, the differences from the first embodiment will be mainly described, and the same portions as those in the first embodiment will be denoted by the same reference numerals. In the first embodiment, the heat medium is cooled by the heat exchanger 5 and the refrigerator 6, and the heat medium condenser 3 and the second condenser 20 are cooled to the same temperature. On the other hand, in the second embodiment, the second heat storage medium (referred to as the second heat medium storage tank 22a) is provided with a second cooling unit, and the second unit is provided with a cooling device. The first-cooling machine 33 cools the second condensing pipe (hereinafter referred to as the second condensing pipe 2〇3) to cool the second condensing pipe 20a at a temperature lower than that of the condensing pipe 3. With such a configuration, low-boiling hydrocarbons such as diners and pentanes can be effectively liquefied in the second condensing duct 20a. Further, since the second condensation tube 2〇at & moving air containing concentrated gasoline vapor does not contain a minute, the moisture in the gas is frozen inside the second condensation tube 20a, so there is no The moisture in the internal gas of the condenser tube 2〇a is frozen, and the flow of the gas in the second condenser tube 20a is stagnated. Therefore, the gasoline vapor recovery device 100a can efficiently recover the low-boiling point enthalpy contained in the separated concentrated gasoline vapor, and can be a miniaturized device. (Embodiment 3) Fig. 4 is a schematic structural view showing an overall structure of a gasoline vapor recovery device 100b according to Embodiment 3 of the present invention. According to Fig. 4, the structure of the gasoline vaporization recovery apparatus 10 Ob and the flow of gasoline vapor will be described. This gasoline vapor recovery device 100b is also an embodiment! The gasoline vapor recovery unit Ο 100 is the same 'gasoline steam is cooled and recovered by the condensation tube 3, and the functions of the two adsorption separation towers for adsorbing or separating the gasoline vapor are appropriately switched to recover (adsorb) and reuse (separate) the gasoline vapor. Attack. In the third embodiment, the same points as those of the first embodiment and the second embodiment are denoted by the same reference numerals, and the same reference numerals are given to the same portions as those of the first embodiment and the second embodiment. In the first embodiment and the second embodiment, the condensing device (second condensing pipe) for condensing the air containing the separated concentrated gasoline vapor is separately provided, and the gasoline vapor to be taken in from the oil supply device 1 is contained. The air is condensed 23 201034741 Condensing device (condensation alarm can be... In the third embodiment, the gas flow 41 is provided as a ni body supply device for changing the air flow rate of the air containing the gasoline vapor, and will be separated from the separation tower 8 After the concentrated steam is mixed with the gasoline vapor taken in from the oil supply device, it is condensed. e J A, in the gasoline vapor recovery unit 1〇〇b, no gasoline vapor suction pump 2, second condensation tube is not provided. a second heat medium storage tank, a second heat exchanger, a first-freezer, a gasoline vapor compression pump, a second gas-liquid separator, and a second pressure controller, but connect the exhaust gas discharge pipe to the valve B1 The gas flow rate variable 41 is a device that changes the flow rate of the gasoline vapor-containing gas taken in from the oil supply device 1. The operation of the gasoline vapor recovery device 丨〇〇b will be described. In plus In the station, the oil supply is carried out irregularly. Therefore, during a limited time of oil supply, the flow rate variable pump 41 is driven by the large flow motor, and the gasoline vapor near the nozzle omitted from the drawing of the apparatus 1 is recovered. On the other hand, 'when no oil is supplied' Μ B1, closed, the flow variable pump is driven by a small flow motor, whereby the air containing concentrated gasoline is sucked from the separation tower 8 by the suction pump n, via the gas The variable flow pump 41 is supplied to the condensing pipe, that is, when the gasoline vapor recovery device 1b is not supplied with oil, only the air containing the separated concentrated gasoline vapor is condensed by the condensing pipe 3. In the steam recovery device 100b, low-boiling hydrocarbons in the air containing the separated concentrated sulphur vapor can be efficiently recovered. Therefore, by performing the separation operation for a long period of time, the gasoline component accumulated in the adsorption separation column can be reduced by 24 201034741 is less, and the amount of adsorption in the next step is increased. However, since the operation time of the suction pump U and the gas flow variable pump 41 is increased, the energy consumption is also increased. Therefore, when the suction pump u is actuated for a predetermined time When the attraction fruit 11 is stopped, the adsorption separation column 7 and the adsorption separation column 8 can be switched at this time. Thus, in addition to continuously supplying the gasoline vapor from the oil supply device i, the gasoline vapor discharged from the gas-liquid separator 9 can be discharged. The air is supplied to the adsorption separation column which does not adsorb the per-gasoline component, and the gasoline vapor can be adsorbed and removed efficiently. That is, when the stop time of the oil supply device 1 is longer than the operation time of the suction miller i, the condensation pipe 3 is used. The low-boiling carbonized carbon which is not condensed is supplied to the adsorption separation column (for example, the adsorption tower 7) in which the gasoline component does not remain. Therefore, the low-boiling hydrocarbon can be efficiently adsorbed to the adsorption separation column, and can have a filling in the adsorption separation column. The effect of the amount of adsorbent used is small. As described above, the gasoline vapor recovery device 100b is an inexpensive and compact device. Further, the features of the first embodiment and the features of the embodiment "state 2" or both are applicable to the embodiment 3. (Embodiment 4) Fig. 5 is a schematic structural view showing the overall circuit structure of the gasoline vapor recovery device 100c of the embodiment 4 of the present invention. According to Fig. 5, the configuration of the gasoline vapor recovery unit 100c and the flow of gasoline vapor will be described. The π oil vapor recovery device 100c is the same as the gasoline vapor recovery device 100 of the first embodiment, and the gasoline vapor is cooled and recovered in the condensing pipe 3, and the function of the adsorption separation column with or without the gasoline vapor is appropriately switched and recovered (adsorption). ) and reuse (separation) devices. In the fourth embodiment, 25 201034741 will be described focusing on points different from the first to third embodiments, and the same portions as those in the first to third embodiments will be denoted by the same reference numerals. In the case of the gas flow variable pump 41 in which the gas flow rate of the air containing the gasoline vapor is set, the gas discharge port 41 is provided in the gas outlet of the gas-liquid separator 9 on the other hand. The second heat exchanger 52 (freezer) of the third freezer 51 that constitutes the flute element of the desired one will flow out from the sputum separator 9 via the third sputum-swapping prize. Gasoline steam cooling. That is, although the 鈇x is Chu, the person fc is not 6 and the first - the congeal tube, the second thermal media storage

Storage tank, second heat exchanger, 筮_, person, shotgun first cold/east machine, gasoline vapor compression pump, first-gas-liquid separation and second foolish six: oysters award ^ Α Α ω a pressure The characteristics of the control|§ are the same as those of the gasoline vapor recovery apparatus 100b of the second embodiment, but the characteristics of the gas flow variable pump 41 and the gasoline vaporized π suction pump 2 are different from those of the third embodiment. With this configuration, the two gas containing gasoline vapor flowing out of the gas-liquid separation $9 is cooled by the first heat master converter 52. Thereby, in the adsorption separation column 7 and

The adsorption separation column 8 + can lower the temperature of the air containing gasoline vapor. Therefore, the removal ability of the low boiling point hydrocarbon in the adsorptive separation column 7 and the adsorptive separation column 8 can be made large. Thereby, the gasoline vapor recovery unit 丨〇〇c can efficiently liquefy the gasoline vapor. Further, by adding the metal granules to the adsorption separation column γ and the adsorption separation column 8 (the first embodiment to the third embodiment, the fifth embodiment to the seventh embodiment are the same), the cooling performance of the adsorbent can be improved, and the adsorption performance can be further improved. Adsorption removal of boiling point hydrocarbons. The heat transfer of the metal granules is good as aluminum and copper which are not corroded by gasoline vapor. Further, any one or a plurality of the embodiments 丨 to 3 are applicable to the fourth embodiment. [Embodiment 5] FIG. 6 is a schematic structural view showing the overall structure of a gasoline vapor recovery device 100d according to Embodiment 5 of the present invention. The configuration of the gasoline vapor recovery unit 10d and the flow of gasoline vapor will be described based on Fig. 6'. The gasoline vapor recovery unit 10d is the same as the gasoline vapor recovery unit 1 of the first embodiment. The gasoline vapor is cooled and recovered by the condensation tube 3, and the adsorption separation towers for adsorbing or separating and separating the oil vapor are appropriately switched. A device that recovers (adsorbs) and reuses (separates) the function. In the fifth embodiment, the same points as those in the first to fourth embodiments are denoted by the same reference numerals, and the same portions as those in the first to fourth embodiments are denoted by the same reference numerals. As shown in Fig. 6, the gasoline vapor recovery unit 丨〇〇d is connected to the gas outlet of the gas-liquid separator 9 and the second condenser 63, and is provided with a second gasoline vapor compression pump 61 serving as a compression pump. That is, in the gasoline vapor recovery device 丨〇〇d, the gasoline-containing air passing through the condensing pipe 3 and the gas-liquid separator 9 is further compressed by the first oil-steaming/squeezing pump 61, and supplied to the second condensing unit. Tube 63. The second gasoline vapor compression pump 61 again compresses the second gas containing the gasoline vapor π and supplies it to the second condenser 63' in the second heat medium storage tank 64 to condense the remaining low boiling point hydrocarbon. The gasoline vapor-containing air condensed by the low boiling point hydrocarbon is supplied to the adsorption separation column 7 or the adsorption separation column 8 via the second gas-liquid separator 62. Further, when the comparison reaches the target pressure in one section and the target pressure in the second stage, the amount of gasoline vapor supplied to the adsorptive separation column 7 or the adsorptive separation column 8 does not change because the arrival pressure is the same. Therefore, in the second-stage compression, since the amount of gas containing the gasoline vapor in the second stage of the liquefied gasoline component in the second stage is changed to V, the energy used in compressing the air containing the gasoline vapor can be changed. less. Further, by supplying the gasoline vapor-containing air which has been deaerated to remove the low boiling point hydrocarbons to the (four) dosing 7 or the suction off the column 8, the low boiling point hydrocarbon which must be removed in the adsorptive separation column 7 or the adsorptive separation column 8 can be reduced. Therefore, the adsorbent charged in the adsorptive separation column 7 or the adsorptive separation column 8 can be reduced. Therefore, a plurality of condensing devices (a condensing device composed of a condensing official 3 and a condensing device comprising a second condensing pipe 63) are provided by the retort recovery device 10, and the compression of the gasoline-containing vapor is reduced by the two-stage compression. The necessary energy of the air, while efficiently liquefying and removing low-boiling tantalum carbide, can efficiently and efficiently recover gasoline vapor. Further, any one or a plurality of the first to fourth embodiments are applicable to the fifth embodiment. (Embodiment 6) Fig. 7 is a schematic structural view showing the overall structure of a gasoline vapor recovery device 100e according to Embodiment 6 of the present invention. According to Fig. 7, the structure of the gasoline vapor recovery unit 1 〇〇d and the flow of gasoline vapor will be described. The gasoline addition eight recovery device 1 is the same as the gasoline vapor recovery device 1 of the first embodiment. 'The gasoline vapor is cooled and recovered in the condensation pipe 3, and the two adsorption separation columns for adsorbing or separating the gasoline vapor are appropriately switched. A device that recovers (adsorbs) and reuses (separates) functions. In the sixth embodiment, the same points as those in the first to fifth embodiments will be mainly described, and the same portions as those in the first to fifth embodiments will be denoted by the same reference numerals. As shown in Figure 7, the gasoline vapor recovery unit! 00e has a low-boiling point hydrocarbon adsorption separation column 71 as a second adsorption separation device and as an adsorption separation column 72 for a low-boiling hydrogen sulfide adsorption and separation unit 72, as for the adsorption separation column 7 and adsorption The air discharged from the separation tower 8 containing a low concentration of gasoline steam/fly. That is, the "gas containing gasoline vapor discharged from the adsorption separation column 7 which is operated as an adsorption column is supplied to the adsorption separation column 71 for low-boiling hydrocarbons which operates as an adsorption column, and the low-boiling hydrocarbon is removed and discharged. To the atmosphere. The adsorbent charged in the adsorptive separation column 71 for low boiling point hydrocarbons and the adsorptive separation column 72 for low boiling point hydrocarbons is a ruthenium ruthenium having a pore diameter of 5 to 1 angstrom, and the zeolite alone or in a mixture thereof. Thereby, low boiling point hydrocarbons are efficiently adsorbed. Further, the switching between the adsorption separation column 71 for low-boiling hydrocarbon hydrocarbons and the adsorption separation column 72 for low-boiling hydrocarbons, and the switching between the adsorption separation column 7 and the adsorption separation: 8 are based on the operation of the gasoline vapor suction pump 2 and the suction pump 11. Knife time. Βρ ′ When the integration time reaches a predetermined time, for example, the adsorption separation column 7 and the adsorption separation column 8 are simultaneously switched with the adsorption separation column for low-boiling hydrocarbons and the adsorption separation column 72 for low-boiling hydrocarbons. Further, for the separation, in order to suppress the re-adsorption, it is preferable that the adsorption separation column 7 and the adsorption separation are as follows: = the point of the hydrocarbon is separated from the column 72 by the absorption point of the carbonization center adsorption separation column 72 instead of the tandem separation. Then, 'the (four) point of the hydrocarbon treatment time 71 and the low boiling = adsorption separation column 72 adsorption (to (four) point hydrocarbon; charge: attached separation tower 7 and adsorption separation tower 8) and in addition to the adsorption separation tower = plus Low boiling point hydrocarbon sequestration separation ^ == is compared with adsorption separation column 72. In the air containing gasoline vapor from the condensing pipe 3, the gas contains several tens of carbonized carbons. Therefore, the adsorbent having a low boiling point hydrocarbon can adsorb a molecule having a relatively small molecular diameter, but the macromolecule cannot be adsorbed. Therefore, when the adsorption separation column 71 and the low boiling point hydrocarbon are adsorbed by the adsorption separation column 72 at a low boiling point, the leakage of hydrocarbon having a large molecular diameter becomes faster. On the other hand, in the case of the adsorption separation column 71 for low-boiling hydrocarbons and the adsorption separation column 72 for low-boiling hydrocarbons, in addition to the adsorption separation column 7 and the adsorption separation column 8, carbon nanotubes having a large molecular diameter are adsorbed. The separation column 7 and the adsorptive separation column 8 are removed, and the hydrocarbon having a small molecular diameter is removed by the adsorption separation column 71 and the low-boiling point hydrocarbon by the adsorption separation column 71 with the low-boiling carbonization ruthenium. Therefore, it is possible to efficiently adsorb and remove hydrocarbons in the air containing gasoline vapor. As described above, the gasoline vapor recovery device 1 〇〇e is provided with an adsorption separation column packed with different adsorbents in series, and the two-stage adsorption can efficiently remove hydrocarbons, and the gasoline vapor can be efficiently recovered. Further, any one or a plurality of the embodiments 1 to 5 are applicable to the embodiment 6. (Embodiment 7) Fig. 8 is a schematic structural view showing the overall structure of a gasoline vapor recovery device 100 f of Embodiment 7 of the present invention. According to Fig. 8, the structure of the gasoline vapor recovery unit 1 〇〇f and the flow of gasoline vapor will be described. The gasoline vapor recovery device 1 〇0 f is the same as the gasoline vapor recovery device 1 of the first embodiment. 'The gasoline vapor is cooled and recovered in the condensing pipe 3, and the functions of the adsorption separation column for adsorbing or separating the gasoline vapor are appropriately switched. A device that recovers (adsorbs) and reuses (separates). Further, in the seventh embodiment, the points different from the first to sixth embodiments will be mainly described, and the same portions as those in the first to sixth embodiments of the present invention will be given the same reference numerals.

The switching of the adsorption point separation tower 71 and the low column 72 of the low-fossil hydrogen hydrocarbon and the gas flow rate of the adsorption separation tower 7 and the gasoline vapor suction pump 2 and the suction pump 11 are set in the embodiment 7 to change the gas flow rate. The variable pump 41, the adsorption 8 and the low boiling point hydrocarbon are separated independently from the adsorption separation column 72 by the adsorption separation column 71 and the low boiling point hydrocarbon. By providing the gas flow variable pump 41, the gasoline components adsorbed to the adsorptive separation column 7 and the adsorptive separation column 8 and the low-boiling-point hydrocarbon adsorption separation column 71 and the low-boiling carbon-hydrogen hydrogen and the separation column 72 are separated and regenerated. effect. Therefore, the gasoline vapor recovery unit i 0 0 f can efficiently recover the low-boiling carbonized nitrogen contained in the separated concentrated gasoline vapor, and can be a compact device. In addition, any one or a plurality of the first to sixth embodiments are applied to the embodiment. [Brief Description of the Drawings] Fig. 1 is a schematic structural view showing the overall circuit structure of the gasoline vapor recovery device of the first embodiment. Fig. 2 is a schematic view showing the structure of another structure of the gasoline vapor recovery device. Fig. 3 is a schematic view showing the overall structure of the gasoline vapor recovery device of the second embodiment. Fig. 4 is a schematic structural view of the entire structure of the gasoline vapor recovery apparatus of the third embodiment. Fig. 5 is a schematic structural view showing the overall configuration of a gasoline vapor recovery device of the fourth embodiment. Fig. 6 is a schematic structural view showing the overall configuration of a gasoline vapor recovery device of the fifth embodiment. Fig. 7 is a schematic structural view showing the overall configuration of a gasoline vapor recovery apparatus of the sixth embodiment. Fig. 8 is a schematic structural view showing the overall configuration of the gasoline vapor recovery apparatus of the seventh embodiment. 0 Figure 9 is a graph showing the relationship between the composition of gasoline and the amount of each machine in the prior art. Fig. 1 is a graph showing the relationship between the gasoline component corresponding to the length of the oil supply time and the amount of each machine in the prior art. Fig. 11 is a graph showing the saturation concentration of the saturated concentration of the gasoline component at 〇·3 MPa. The line graph is a saturated concentration indicating the saturation concentration of the gasoline component. [Main component symbol description] 1~ oil supply device; 2~ gasoline vapor suction pump; 3~ condensation tube; 4~ thermal media storage tank; Converter; 32 201034741 6 ~ freezer; 7, 8 ~ adsorption separation tower; 9 ~ gas-liquid separator; 10 ~ liquid circulation pump; 11 ~ suction pump; 12 ~ gasoline tank; 13 ~ pressure controller; Steam air supply pipe; ❹ 15~ purified air discharge pipe; 16~ exhaust gas inflow pipe; 17~ exhaust gas discharge pipe; 1 8~ gas-liquid mixed gasoline outflow pipe; 1 9~ gasoline vapor compression pump; 20~ second Condenser tube; 20a~ second condensation tube; Q 21~ second gas-liquid separator; 22~ second heat medium storage tank; 22a~ second heat medium storage tank; 23~ second pressure controller; 31~ heat medium Storage tank; 32~second heat exchanger; 33~second freezer; 41~gas flow variable pump; 51~third freezer; 33 201034741 52~ third heat exchanger; 61~ gasoline vapor compression pump; 62~ second gas-liquid separation benefit, 63~ second Condensation tube; 64~ second heat medium storage tank; 71, 72~ low boiling point hydrocarbon adsorption separation tower; 100, 100a, 100b, 100c, 100d, 100e, 100f~ gasoline vapor recovery unit; B1, B 2~ valve ; B3 ~ separation valve; B4 ~ adsorption discharge valve; B5 ~ mass flow controller; B6 ~ adsorption inflow valve; B 7 ~ valve 0

34

Claims (1)

201034741 VII. Patent application scope: 1. A gas-like hydrocarbon recovery device comprising: a condensing device for cooling gasoline vapor; a gas-liquid separator 'located on the downstream side of the condensing device, cooled and condensed and liquefied in the condensing device a gasoline-liquid and unliquefied gasoline-steam separation and adsorption device is disposed on the downstream side of the gas-liquid separator, and adsorbs and separates the gasoline vapor separated by the gas-liquid separator; and a second condensation device is connected to In the above-described adsorption separation device, the gasoline vapor adsorbed and separated by the adsorption separation device is supplied thereto to cool the gasoline vapor. 2. The gas-like hydrocarbon recovery apparatus of claim 2, wherein a heat medium storage tank is provided for storing a heat medium for cooling the condensing unit and the second condensing unit. 3. A gas-like hydrocarbon recovery device as claimed in claim 2, wherein the condensing device and the second condensing device are disposed in a common or separate heat medium storage tank. 4. If the gas-like carbonized gas described in claim 2 or 3 is applied, it further includes - cold; the east machine is configured to store the hot cross section of the above-mentioned machine in the upper I thermal medium storage tank. The above thermal media. 5. As claimed in the patent application No. 1 to 4, a hydrocarbon recovery device, the gas-like condensation-receiving door of the separation device described above, and the second vapor pressure fruit, supplied to the adsorption separation device ^Prepressing' and providing a pressure controller for adjusting the pressure in the second condensing device described above on the downstream side of the second condensing device. 6. A device for recovering a milk-like carbonized nitrogen, comprising: a deformable gas supply device capable of changing a gas flow rate of the gasoline vapor to be attracted; ^ a condensing device for supplying gasoline vapor from the deformable gas supply device Cooling; a gas-liquid separator disposed on the downstream side of the condensing device, and the condensed liquefied gasoline liquid is separated from the unliquefied gasoline vapor by the condensing device; and the // separating device is disposed in the gas The liquid separation is crying from the gas downstream of the a_I rolling agricultural knife separator'', and the gasoline vapor separated by the above gas-liquid separator is adsorbed and separated. 7. A gas-like hydrocarbon recovery device comprising: a condensing device for cooling the gasoline vapor; a gas-liquid separator, disposed on the downstream side of the condensing device, and condensing and liquefying the gasoline in the upper condensing device; , the liquefied gasoline vapor j·, +, the production of the mouth... the bottle-side, the D-night separator separates and flows out of the gasoline vapor; and the adsorption separation device is located in the above-mentioned cold-cooled 4 The downstream side 'adsorbs and separates the gasoline vapor cooled by the 7-freezer. . The recovery and cleavage of oxygenated carbonized chlorine, the scooping-condensing device 'cools the gasoline vapor; the gas-liquid separator, which is disposed on the downstream side of the condensation device and the downstream side, and condenses and liquefies in the cold part of the upper device The gasoline liquid is separated from the unliquefied gasoline vapor 201034741; the compressed fruit is 'pressurized to compress a gasoline vapor flowing from the gas-liquid separator; and '' a second condenser is disposed on the downstream side of the gas of the gas-liquid separator The gasoline vapor separated by the above-described gas-liquid separator and pressurized by the above-described compression spring is cooled. 9. The gas-like hydrocarbon recovery device of claim 8, further comprising: a 〇__ Chu Yiyi gas-liquid separator disposed on a downstream side of the second condensing device to cause the first condensing device The cooled and condensed liquefied gasoline liquid is separated from the unliquefied gasoline vapor; and the adsorption is an off-gas device, and the gasoline downstream of the second gas-liquid separator is disposed on the downstream side of the gas-liquid separator. Separation. 10. A gas-like hydrocarbon recovery device comprising: a condensing device 'cooling gasoline vapor; a gas-liquid separator, disposed on a downstream side of the condensing device, and condensing and liquefying the gasoline liquid in the condensing device Unliquefied gasoline vapor separation; an adsorption separation device disposed on the downstream side of the gas of the gas-liquid separator, adsorbing and separating the gasoline vapor separated by the gas-liquid separator; and a second adsorption separation device The gasoline vapor flowing out of the adsorption separation device is adsorbed and separated. The gas-like hydrocarbon recovery device according to the invention, wherein the second adsorption separation device is filled with a sorbent having a pore diameter of 5 3 Ί 201034741 〜 1 〇. 12. The apparatus for recovering gaseous hydrocarbons according to claim 1 or claim 1, further comprising a deformable gas supply device disposed on an upstream side of the condensing device to change the gasoline vapor to be sucked Gas flow. A method for recovering a gas-like carbonized argon, which uses the gas-like hydrocarbon recovery device according to any one of claims 1 to 7 and 9 to 12, to separate the adsorption during the period when no oil is supplied. The two-gas condensation containing concentrated gasoline vapor is treated by mixing the air containing the attracted gasoline vapor with the air containing the adsorbed separated concentrated gasoline vapor during the oil supply period. 14. A method for recovering a gaseous hydrocarbon, which uses the gas-like hydrocarbon recovery device described in any one of the above-mentioned patents 1 to 12 to perform adsorption of the above adsorption separation device in a time of & Switching between the device and the separating device. , 丄〇 A丄4 items traced I The receiving method is set at the timing (4) based on the integral value of the operating time of the gas-like carbonitride device. 38