JP5693448B2 - Gaseous hydrocarbon recovery apparatus and method - Google Patents

Description

  TECHNICAL FIELD The present invention relates to an apparatus and method for recovering gaseous hydrocarbons contained in an atmospheric emission gas, and more particularly to an apparatus and method for processing and recovering gasoline vapor (hereinafter referred to as gasoline vapor) that leaks during gasoline refueling. Is.

  In a conventional hydrocarbon recovery system and method using adsorbent and desorbent, the gas generated from the exhaust gas source (exhaust gas containing about 40 vol% gasoline vapor) is condensed from the exhaust gas feed pipe with blower or self-pressure. After the gasoline vapor is partially liquefied in the condenser, air containing gasoline vapor that has not been liquefied is sent to the adsorption tower, and the treated exhaust gas that has finished the adsorption process is removed from the adsorption tower (desorption). After switching to the process, there is one that is released into the atmosphere as air (clean gas) containing 1 vol% or less of gasoline vapor from the top of the desorption tower) through a discharge pipe.

  Then, 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 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 being desorbed 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 the exhaust gas.

  By setting it as such a structure, gasoline vapor can be collect | recovered as almost all liquid gasoline. Therefore, in the apparatus and method for recovering gaseous hydrocarbons having such a configuration, the concentration of gasoline vapor discharged from the adsorption tower is sufficiently low, and can be reduced to a level that does not cause air pollution (for example, patents). Reference 1). In the technique of Patent Document 1, since moisture in the air is mixed in the first condensing device, when the cooling temperature is set below the freezing point, the water is frozen in the first condensing device and the first condensing device is blocked. It will end up. Therefore, it was necessary to set the cooling temperature of the first condensing device above the freezing point.

JP 2006-198604 A (pages 4 to 8, FIG. 2, and pages 9 to 16, FIG. 10)

  However, at such a set temperature, low boiling point hydrocarbons such as butane and isobutane, which are the main components of gasoline vapor, do not liquefy and flow into the adsorption tower as they are, so the time until the gasoline vapor leaks from the adsorption tower Will shorten the adsorption tower switching time. Further, in order not to shorten the switching time of the adsorption tower, it is necessary to enlarge the adsorption tower, that is, to increase the amount of the adsorbent filled in the adsorption tower, so that the apparatus becomes large.

  Further, in the method of mixing the gasoline vapor sucked from the nozzle of the fueling device as in Patent Document 1 and the gasoline vapor desorbed from the adsorption tower and condensing with the condensing device, the gasoline vapor sucked from the nozzle has a relatively low concentration. The concentrated gasoline vapor desorbed from the adsorption tower will be mixed. For this reason, low-boiling hydrocarbons such as butane and isobutane with a high saturated vapor pressure concentration also have a low concentration in the gas, and are not condensed in the condensing tower, but are supplied again to the adsorption tower. Not only will it get worse, it will waste energy.

  The present invention has been made to solve the above-described problems, and has an object to provide a gaseous hydrocarbon recovery apparatus and method capable of efficiently liquefying gasoline contained in gasoline vapor. It is.

The recovery apparatus for gaseous hydrocarbons according to the present invention includes a condensing device for cooling gasoline vapor, a gasoline liquid that is provided downstream of the condensing device, cooled by the condensing device, and condensed and liquefied, and a gasoline vapor that has not been liquefied. A gas-liquid separator that is connected to the gas-liquid separator, an adsorption / desorption device that adsorbs and desorbs the gasoline vapor separated by the gas-liquid separator, and is connected to the adsorption / desorption device. And a second condensing device that is supplied with the gasoline vapor desorbed by the adsorption / desorption device and cools the gasoline vapor, and stores the heat medium that stores the heat medium that cools the condensing device and the second condensing device. A heat medium storage tank for storing a heat medium for cooling the second condensing device in the heat medium storage tank, and heat for cooling the condensing device in the heat medium storage tank in the adsorption / desorption device. Wherein the supply of heat medium of the heat medium storage tank for storing the body in parallel.

  The method for recovering gaseous hydrocarbons according to the present invention is a method for recovering gaseous hydrocarbons using the above-described gaseous hydrocarbon recovery device, which contains concentrated gasoline vapor desorbed in a time zone in which refueling is not performed. In the time zone in which air is condensed and refueling is performed, the sucked gasoline vapor-containing air and the desorbed concentrated gasoline vapor-containing air are mixed and processed.

  A method for recovering gaseous hydrocarbons according to the present invention is a method for recovering gaseous hydrocarbons using the above-described gaseous hydrocarbon recovery device, wherein the adsorption and desorption devices of the adsorption / desorption device are desorbed every predetermined time. The apparatus is switched.

  According to the gaseous hydrocarbon recovery device of the present invention, since the second condenser for condensing the gasoline vapor desorbed from the adsorption / desorption device is provided, the gasoline vapor desorbed from the adsorption / desorption device can be condensed individually. Therefore, low boiling point hydrocarbons such as butane and isobutane having a high saturated vapor pressure concentration by mixing gasoline vapor sucked from the nozzle with concentrated gasoline vapor desorbed from the adsorption / desorption device. Therefore, it is possible to prevent the low-boiling hydrocarbons from being condensed and recovered with high efficiency.

  According to the method for recovering gaseous hydrocarbons according to the present invention, the function of the adsorption / desorption device as the adsorption device and the function as the desorption device are appropriately switched, so that the improvement of the recovery efficiency of gasoline vapor is realized. it can.

1 is a schematic configuration diagram illustrating an overall circuit configuration of a gasoline vapor recovery device according to Embodiment 1. FIG. It is a schematic block diagram which shows another structure of a gasoline vapor collection | recovery apparatus. It is a schematic block diagram which shows the whole structure of the gasoline vapor collection apparatus which concerns on Embodiment 2. FIG. FIG. 6 is a schematic configuration diagram illustrating an overall configuration of a gasoline vapor recovery device according to a third embodiment. It is a schematic block diagram which shows the whole structure of the gasoline vapor recovery apparatus which concerns on Embodiment 4. It is a schematic block diagram which shows the whole structure of the gasoline vapor collection apparatus which concerns on Embodiment 5. It is a schematic block diagram which shows the whole structure of the gasoline vapor recovery apparatus which concerns on Embodiment 6. FIG. 10 is a schematic configuration diagram illustrating an overall configuration of a gasoline vapor recovery device according to a seventh embodiment. It is a graph which shows the relationship between the gasoline component and the quantity for every apparatus in a conventional system. It is a graph which shows the relationship between the gasoline component according to the length of the oiling time in a conventional system, and the quantity for every apparatus. It is a saturation concentration diagram which shows the saturation concentration at the time of 0.3 Mpa of a gasoline component. It is a saturation concentration diagram which shows the saturation concentration at the time of 5 degreeC of a gasoline component.

Hereinafter, embodiments of the present invention will be described with reference to the drawings.
Embodiment 1 FIG.
FIG. 1 is a schematic configuration diagram showing an overall circuit configuration of a gasoline vapor recovery device 100 according to Embodiment 1 of the present invention. FIG. 2 is a schematic configuration diagram showing another configuration of the gasoline vapor recovery device 100. Based on FIG.1 and FIG.2, the circuit structure of the gasoline vapor collection apparatus 100 which is a gaseous hydrocarbon collection | recovery apparatus, and the flow of a gasoline vapor are demonstrated. In addition, in the following drawings including FIG. 1, the relationship of the size of each component may be different from the actual one.

  The gasoline vapor recovery device 100 is installed in a gas station or the like together with the fuel supply device 1 for supplying gasoline to an automobile or the like. The gasoline vapor recovery device 100 cools and recovers the gasoline vapor sucked from the vicinity of the oil supply section with the condensation pipe 3 and also absorbs or desorbs the gasoline vapor (an adsorption / desorption tower 7 and an adsorption / desorption tower 8). The gas vapor is recovered (adsorbed) and reused (desorbed) by appropriately switching the functions of the two adsorption / desorption towers.

  The gasoline vapor recovery apparatus 100 includes a gasoline vapor suction pump 2, a condenser tube 3, a heat medium storage tank 4, a heat exchanger 5, a refrigerator 6, and two adsorption / desorption towers (an adsorption / desorption tower 7, an adsorption / desorption tower 7). Desorption tower 8), gas-liquid separator 9, liquid circulation pump 10, suction pump 11, gasoline tank 12, pressure controller 13, gasoline vapor feed pipe 14, purified air discharge pipe 15, and purge gas inflow A pipe 16, a purge gas discharge pipe 17, a gas-liquid mixed gasoline outflow pipe 18, a gasoline vapor compression pump 19, a second condensing pipe 20, a second gas-liquid separator 21, and a second heat medium storage tank 22 , A second pressure controller 23.

  The gasoline vapor suction pump 2 is for sucking gasoline vapor generated in the vicinity of an oil supply portion of the fuel supply device 1 into the gasoline vapor recovery device 100 through a nozzle (not shown). The condensing pipe 3 cools the sucked gasoline vapor and condenses it. The heat medium storage tank 4 stores the heat medium such as brine for cooling the condensing pipe 3 while the condensing pipe 3 is accommodated therein. The heat exchanger 5 constitutes a part of the refrigerator 6 and is accommodated in the heat medium storage tank 4 to cool the heat medium in the heat medium storage tank 4. The refrigerator 6 includes a refrigeration cycle, and supplies refrigerant to the heat exchanger 5 that constitutes the refrigeration cycle.

  The adsorption / desorption tower 7 and the adsorption / desorption tower 8 are filled with an adsorbent (for example, silica gel, zeolite, activated carbon, etc.) for adsorbing and removing gasoline vapor in the gasoline vapor-containing air discharged from the condensation pipe 3. Has a function as an adsorption tower for adsorbing gas and a function as a desorption tower for desorbing gasoline vapor. In FIG. 1, the adsorption / desorption tower 7 operates as an adsorption tower (hereinafter sometimes referred to as an adsorption tower 7), and the adsorption / desorption tower 8 is referred to as a desorption tower (hereinafter sometimes referred to as a desorption tower 8). As an example).

  The gas-liquid separator 9 is connected to the downstream side of the condensing pipe 3, and gas-liquid separates the gasoline liquid and the gasoline vapor liquefied in the condensing pipe 3. The liquid circulation pump 10 is connected to the heat medium storage tank 4 and the two adsorption / desorption towers, and supplies the heat medium cooled by the heat exchanger 5 to the adsorption / desorption tower 7 and the adsorption / desorption tower 8. . The suction pump 11 is provided in a pipe connected to the two adsorption / desorption towers, and sucks and desorbs the gasoline vapor adsorbed by the adsorbent in the adsorption / desorption tower 7 and 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 provided in the purified air discharge pipe 15 connected to the two adsorption / desorption towers, and has a function of adjusting the pressure in the two adsorption / desorption towers. The gasoline vapor feed pipe 14 is a pipe that connects the gas-liquid separator 9 and the two adsorption / desorption towers, and guides the gasoline vapor separated by the gas-liquid separator 9 to the two adsorption / desorption towers. The purified air discharge pipe 15 is connected to the two adsorption / desorption towers, and is a pipe that adsorbs gasoline vapor and sends the air discharged from the adsorption / desorption tower to the atmosphere.

  The purge gas inflow pipe 16 is connected to two adsorption / desorption towers, and in order to use a part of the clean gas discharged from the adsorption / desorption tower 7 or the adsorption / desorption tower 8 to the atmosphere as the purge gas, the adsorption / desorption tower 8 or the adsorption / desorption tower 16 is used. This is a pipe for sending to the desorption tower 7. The purge gas discharge pipe 17 is a pipe that connects the suction pump 11 and the two adsorption / desorption towers, and conducts the purge gas after desorption of the adsorption / desorption tower 7 or the adsorption / desorption tower 8 to the second heat medium storage tank 22. The gas-liquid mixed gasoline outflow pipe 18 is a pipe connected to the condensing pipe 3 and the gas-liquid separator 9. The gasoline vapor compression pump 19 is provided between the suction pump 11 and the second heat medium storage tank 22 and compresses the concentrated gasoline vapor-containing air discharged from the suction pump 11.

  The second condensing pipe 20 is connected to the purge gas discharge pipe 17 and condenses the gasoline component in the concentrated gasoline vapor-containing air compressed by the gasoline vapor compression pump 19. The second gas-liquid separator 21 is connected to the downstream side of the second condensing pipe 20 and gas-liquid separates the gasoline liquid liquefied in the second condensing pipe 20 and the gasoline vapor. The second heat medium storage tank 22 stores the heat medium such as brine for cooling the second condensing pipe 20 while the second condensing pipe 20 is accommodated therein. The second pressure controller 23 is connected to the second gas-liquid separator 21 and adjusts the pressure in the second condensing pipe 20 by adjusting the pressure in the second gas-liquid separator 21.

  Further, in the gasoline vapor recovery device 100, a valve B1 provided between the fuel supply device 1 and the gasoline vapor suction pump 2, a valve B2 provided between the gas-liquid separator 9 and the gasoline tank 12, Desorption valve B 3 provided between the two adsorption / desorption towers and the suction pump 11, Adsorption discharge valve B 4 provided between the two adsorption / desorption towers and the pressure controller 13, and two adsorption / desorption towers An adsorbing inflow valve B6 provided in the middle of the mass flow controller B5 provided in the purge gas inflow pipe 16 connected to the two, the gasoline vapor air supply pipe 14 connected to the two adsorption / desorption towers, and the second A valve B7 provided between the gas-liquid separator 21 and the gasoline tank 12 is provided. In addition, the valve | bulb which is open is painted black, and the valve | bulb which is closed is represented by white (a code | symbol is attached | subjected to ').

  The valve B1 is opened in conjunction with the operation of the fueling device 1. The valve B2 is opened when the gasoline liquid recovered by the gas-liquid separator 9 is supplied to the gasoline tank 12. The desorption valve B3 is opened when the purge gas after desorption of the adsorption / desorption tower 7 or the adsorption / desorption tower 8 is conducted. The adsorption discharge valve B4 is opened and closed to adjust the pressures of the two adsorption / desorption towers. The mass flow controller B5 is opened and closed to adjust the amount of gas flowing through the purge gas inflow pipe 16. The adsorption inflow valve B6 is opened when the gasoline vapor supplied from the gas-liquid separator 9 is conducted. The valve B7 is opened when the gasoline liquid recovered by the second gas-liquid separator 21 is supplied to the gasoline tank 12.

The operation of the gasoline vapor recovery device 100 will be described.
When the fueling device 1 is operated, the valve B1 is opened at the same time, and the gasoline vapor suction pump 2 starts operating. Then, the gasoline vapor (about 40 vol% at normal temperature) generated in the vicinity of the oil supply portion of the fuel supply device 1 is sucked into the gasoline vapor recovery device 100 and is compressed and compressed to about 0.2 to 0.4 MPa, for example. Is inflated. The condenser tube 3 is provided in the heat medium storage tank 4 and is cooled by the heat medium stored in the heat medium storage tank 4. Therefore, the gasoline vapor is cooled when it passes through the condensation pipe 3.

  Usually, the inside of the condensing tube 3 is maintained at about 0 ° C. to 5 ° C., and water contained in gasoline and gas is partially condensed. Then, it flows into the gas-liquid separator 9 and is separated into gas (gasoline vapor) and liquid (gasoline) by the gas-liquid separator 9. By the way, if the operating conditions of the condensing pipe 3 are a pressure of 0.3 MPa, a cooling temperature of 5 ° C., a gas flow rate of 100 L / min, and the gasoline vapor recovery device 100 is operated under these conditions, the gasoline vapor fed to the condensing pipe 3 is used. The concentration of is about 10 vol%.

  As can be seen from the saturated concentration diagram of gasoline vapor (not shown), the saturated gasoline vapor concentration is about 10 vol% at a pressure of 0.3 MPa and a temperature of 5 ° C. Under these conditions, the gasoline vapor concentration is theoretically 10 vol%. It will never be Moreover, the gasoline vapor density | concentration in the exit of the condensation pipe | tube 3 can be reduced by lowering | hanging temperature. However, if the set temperature is below the freezing point, the water contained in the gas freezes in the condensing tube 3 and a problem of clogging of the pipe occurs. Therefore, the set temperature of the condensing tube 3 may be set to about 0 to 5 ° C. desirable.

  Further, when the refueling time reaches a predetermined time, the valve B2 is opened. Thereby, the gasoline liquid collected in the lower part of the gas-liquid separator 9 is returned to the fuel supply device 1 via the gasoline tank 12. Thereafter, when a certain time elapses, the valve B2 is closed, and the gasoline liquid is stored again in the lower part of the gas-liquid separator 9. Thus, since the gasoline tank 12 is provided, it is possible to prevent gasoline vapor from flowing into the gas-liquid separator 9. In this way, the adsorption breakthrough time of the adsorption / desorption tower 7 or the adsorption / desorption tower 8 due to the high concentration gasoline vapor flowing into the adsorption / desorption tower 7 or the adsorption / desorption tower 8 can be prevented. I have to.

  As shown in FIG. 1, in the gasoline tank 12, a certain amount of gasoline liquid is stored in the lower part, and the gasoline liquid separated by the gas-liquid separator 9 flows from the bottom and falls in the gasoline tank 12. It flows from the top to the top. As a result, the gasoline tank 12 has a structure in which gasoline vapor is present at the top. 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. Will not be inflated.

  Gasoline vapor of about 10 vol% that could not be processed by the condenser tube 3 is sent to the adsorption / desorption tower 7 or the adsorption / desorption tower 8 (the adsorption / desorption tower 7 operating as an adsorption tower in FIG. 1) and processed. Therefore, at this time, the detachment valve B3 is open (black), the detachment valve B3 ′ (white) is closed, the suction discharge valve B4 is open (black), and the suction discharge valve B4 ′. (White) is in a closed state, the suction inflow valve B6 is open (black), and the suction inflow valve B6 ′ (white) is controlled in a closed state.

  After the adsorption treatment for an arbitrary time in the adsorption tower 7, it is used as a desorption tower. In this case, the detachment valve B3, the suction discharge valve B4, and the suction inflow valve B6 are closed, and the detachment valve B3 ′, the suction discharge valve B4 ′, and the suction inflow valve B6 ′ are open. Used under control. Further, when the desorption is completed, it is used again as an adsorption tower, and this operation is repeated over time. As described above, the adsorption / desorption switching is performed by switching between the desorption valve B3 and the desorption valve B3 ′, the adsorption discharge valve B4 and the adsorption discharge valve B4 ′, and the adsorption inflow valve B6 and the adsorption inflow valve B6 ′. To control.

  Therefore, the gasoline vapor that could not be processed by the condensation pipe 3 is sent to the adsorption tower 7 through the gasoline vapor supply pipe 14. The adsorption / desorption tower 7 and the adsorption / desorption tower 8 contain an adsorbent that adsorbs gasoline vapor as described above. As the adsorbent for adsorbing gasoline vapor, silica gel having a pore size of 4 to 100 angstrom, synthetic zeolite alone or a mixture thereof is particularly effective. As the gasoline vapor passes through the adsorbent, the gasoline components are adsorbed and removed by the adsorbent, 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.

  Further, as described above, the pressure controller 13 that controls the pressures of the adsorption / desorption tower 7 and the adsorption / desorption tower 8 to a specified value is disposed in the purified air discharge pipe 15 that discharges clean air to the atmosphere. Therefore, the pressure controller 13 maintains the pressure in the adsorption tower 7 at a specified value. In the first embodiment, the adsorption capacity is greatly improved as compared with the case of adsorption at normal pressure because the adsorption is performed using the high-pressure (about 0.3 MPa) exhaust gas of the condensation tube 3.

  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 irrespective of the role of gasoline vapor adsorption / desorption. That is, the operation of the condenser pipe 3 and the cooling system of the two adsorption / desorption towers is always controlled so as to be maintained at a predetermined set temperature. This is because the adsorbent packed 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. Moreover, it is because providing the refrigerator 6 with a large cooling capacity so that it can cool in a short time has a bad influence on equipment cost, and cannot provide an inexpensive gasoline recovery apparatus.

  In addition, by lowering the temperature inside the adsorption tower 7, the adsorption capacity of the adsorbent can be increased, and the amount of adsorbent used can be reduced. Further, since the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are maintained at a predetermined set temperature, 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. It is possible to effectively prevent the gasoline vapor from desorbing from the adsorbent in the desorption tower 7 and the adsorption / desorption tower 8 and increasing the pressure in the adsorption / desorption tower 7 and the adsorption / desorption tower 8.

The process for desorbing gasoline vapor will be described.
When desorbing the gasoline adsorbed on the adsorbent, the suction pump 11 sucks gas from the desorption tower 8 through the purge gas discharge pipe 17 to desorb the gasoline from the adsorbent. At this time, the detaching valve B3 is opened and the detaching valve B3 ′ is closed. At the time of adsorption, the adsorption tower (in this example, the adsorption tower 7) operates at a high pressure of 0.3 MPa, but at the time of desorption, the pressure is reduced to below atmospheric pressure by the suction pump 11. Gasoline is desorbed.

  The desorbed gasoline vapor is compressed by the gasoline vapor compression pump 19 and the second pressure controller 23 and sent to the second condensing pipe 20. The second condensing pipe 20 is provided in the second heat medium storage tank 22, and is cooled by the heat medium stored in the second heat medium storage tank 22. Therefore, the gasoline vapor is cooled when passing through the second condensing pipe 20. Usually, the inside of the second condensing tube 20 is maintained at about 0 ° C. to 5 ° C., and water contained in gasoline and gas is partially condensed. Thereafter, the gas 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. As a result, the gasoline liquid collected in the lower part of the second gas-liquid separator 21 is returned to the fuel supply device 1 via the gasoline tank 12. On the other hand, about 10 vol% of the gasoline vapor that could not be processed by the second condensing pipe 20 is returned to the adsorption tower 7 through the second pressure controller 23 and the gasoline vapor feed pipe 14. That is, the concentrated gasoline vapor taken out from the desorption tower 8 is supplied to the second condensing pipe 20 while maintaining a high concentration state and efficiently liquefied, and the gasoline vapor that has not been liquefied is adsorbed again in the adsorption tower 7. Removed.

  Since only the method using the pressure difference due to the suction of the suction pump 11 at the time of desorption is not so high in desorption efficiency, it is effective to introduce a purge gas from the outside. Therefore, in the first embodiment, a part of the clean gas discharged from the adsorption tower 7 to the atmosphere as the purge gas is sent to the desorption tower 8 through the purge gas inflow pipe 16 'for use. The mass flow controller B5 and the mass flow controller B5 'control the gas flow rate passing through the purge gas inflow pipe 16, and in this case, the mass flow controller B5 is in an open state and the mass flow controller B5' is in a closed state.

  That is, the mass flow controller B5 is in a state where a specified amount of gas can be circulated in an open state, and the mass flow controller B5 'is in a closed state so that no gas flows. In the first embodiment, since the amount of moisture in the gas is sufficiently reduced in the condenser tube 3 at the previous stage, the moisture contained in the purge gas hardly affects the adsorbent in the desorption tower 8.

Switching between the adsorption / desorption tower 7 and the adsorption / desorption tower 8 will be described.
As described above, the gasoline vapor is adsorbed and removed by passing through the adsorption tower 7, so that the gasoline vapor becomes clean air having a gasoline concentration of 1 vol% or less and is released to the atmosphere through the purified air discharge pipe 15. However, as the amount of gasoline vapor supplied to the adsorption tower 7 increases, the adsorption capacity of the adsorption tower 7 gradually decreases. If this state continues and the gasoline concentration at the outlet of the adsorption tower 7 approaches 1 vol%, it is necessary to switch between the adsorption / desorption tower 7 and the adsorption / desorption tower 8.

  At the gas station, refueling is performed irregularly. For this reason, when the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are simply switched over time, depending on the oil supply timing, the adsorption operation is performed only in either the adsorption / desorption tower 7 or the adsorption / desorption tower 8. there is a possibility. If it does so, there exists a possibility that 1 vol% or more of gasoline vapor may be discharged | emitted from the gasoline vapor collection apparatus 100. FIG. Therefore, it is effective to switch between the adsorption / desorption tower 7 and the adsorption / desorption tower 8 by an integrated value of the time during which the gasoline recovery apparatus 100 is operating. That is, when the integrated value of the time during which the gasoline recovery apparatus 100 is operating reaches a predetermined time, the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are switched, the integrated value is reset, and the operation time is again set. Start counting from the beginning.

  In addition, as an index representing the operation of the gasoline vapor recovery device 100, the operation of the gasoline vapor suction pump 2 and the suction pump 11 can be cited. In the gasoline vapor recovery apparatus 100, since the gasoline vapor suction pump 2 and the suction pump 11 are synchronized, there is no problem regardless of which operating time is integrated. Further, as the actual switching timing, even if the integration time reaches the predetermined value, the switching is not performed immediately, but may be performed after a certain time has elapsed.

A cooling control method for the second condensing pipe 20 will be described.
The heat medium in the heat medium storage tank 4 cooled by the refrigerator 6 is supplied to the second heat medium storage tank 22 by the liquid circulation pump 10, thereby cooling the second condensing pipe 20. In addition, although FIG. 1 illustrates the case where the piping through which the heat medium supplied to the desorption tower 8 flows is branched and the heat medium is supplied to the second heat medium storage tank 22, the present invention is limited to this. It is not a thing. That is, it is sufficient that the heat medium is supplied in parallel to the second heat medium storage tank 22, the adsorption / desorption tower 7, and the adsorption / desorption tower 8. Therefore, the supply of the heat medium to the second heat medium storage tank 22 may be branched from a pipe through which the heat medium supplied to the adsorption tower 7 flows, and the outlet of the liquid circulation pump 10 is branched in three directions. May be.

  The reason for supplying the heat medium to the second heat medium storage tank 22, the adsorption / desorption tower 7, and the adsorption / desorption tower 8 in parallel is that the second heat medium storage tank 22, the adsorption / desorption tower 7, the adsorption / desorption are performed. When the supply of the heat medium to the tower 8 is performed in series, the temperature of the heat medium is higher than a predetermined temperature in the last flowing equipment (equipment located at the most downstream side), so the performance in that equipment is This is because the performance of the gasoline vapor recovery device 100 as a whole is lowered.

  A method of condensing the desorbed gasoline vapor, which is a feature of the gasoline vapor recovery device 100 according to Embodiment 1, will be described in comparison with a conventional method. The method of condensing the desorbed gasoline vapor alone is a method in which the gasoline vapor desorbed in the adsorption / desorption tower is condensed independently without being mixed with the gasoline vapor taken in from the fueling device (hereinafter, This method is called). The conventional method to be compared is a method in which the desorbed gasoline vapor is mixed with the gasoline vapor taken in from the fueling device and then condensed.

  FIG. 9 is a graph showing the relationship between the gasoline component (horizontal axis) and the amount of each device (vertical axis) in the conventional method. FIG. 10 is a graph showing the relationship between the gasoline component (horizontal axis) according to the length of the refueling time in the conventional system and the amount (vertical axis) for each device. FIG. 11 is a saturation concentration diagram (temperature [° C.] on the horizontal axis and saturation concentration [vol%] on the vertical axis) showing the saturation concentration of the gasoline component at 0.3 MPa. FIG. 12 is a saturation concentration diagram (saturation concentration [vol%] on the horizontal axis and pressure [MPa] on the vertical axis) showing the saturation concentration of the gasoline component at 5 ° C. Based on FIGS. 9 to 11, the components of gasoline will be described, and the recovery of low-boiling hydrocarbons will be described.

  In FIG. 9, four elements (gasoline tank 12 (a), gasoline vapor compression pump 19 (b), gas-liquid separator 9 outlet (c), and adsorption / desorption tower outlet (d)) of the gasoline vapor recovery apparatus 100 are shown. The amount of gasoline component is shown. In FIG. 9, the amount of the gasoline component at the time of 250 L refueling is shown. FIG. 9 shows that the amount of low boiling point hydrocarbons (C4 hydrocarbon and C5 hydrocarbon) is not reduced by the gas-liquid separator 9. Further, FIG. 9 shows that the amount of the low-boiling hydrocarbon adsorption / desorption tower outlet is not reduced.

  FIG. 10 illustrates the amount (e) of the gasoline component at the adsorption / desorption tower outlet at the time of 50 L refueling and the amount (f) of the gasoline component at the adsorption / desorption tower outlet at the time of 285 L refueling. As shown in FIG. 10, as the refueling time increases, the leakage amount of low boiling point hydrocarbons (especially C4 hydrocarbons such as butane and isobutane and C5 hydrocarbons such as the Oldham ring far end and isopentane) also increases. I understand that. 9 and 10, it can be seen that improving the recovery efficiency of low-boiling hydrocarbons improves the recovery efficiency of the entire gasoline vapor.

  FIG. 11 shows that the recovery efficiency of gasoline vapor can be improved by low temperature use. This principle is utilized both in this method and in the conventional method by cooling the heat medium in the heat medium storage tank with a refrigerator and maintaining the adsorption / desorption tower at a predetermined temperature. From FIG. 12, it can be seen that the saturation concentration of gasoline vapor, particularly the saturation concentration of low-boiling hydrocarbons, depends on the effect of pressure. From FIG. 11 and FIG. 12, it can be seen that the use of low temperature and the use of pressure improve the recovery efficiency of low-boiling point hydrocarbons (second embodiment compression will be described in Embodiment 6).

  In the case where the isobutane concentration in the gasoline vapor-containing air taken in from the fueling device is 40 vol%, the gas flow rate is 70 L / min, the isobutane concentration in the desorbed gasoline vapor-containing air is 70 vol%, and the gas flow rate is 30 L / min. Compare the method with this method. It is assumed that the condensation conditions are a gas pressure of 0.3 MPa and a cooling temperature of 2 ° C. The saturated vapor concentration of isobutane under these conditions is 56 vol%. Therefore, in the conventional system, the isobutane concentration of the gasoline vapor-containing air when mixed is 49 vol%, which is equal to or lower than the saturated vapor concentration. Under such conditions, isobutane cannot be recovered at all.

  On the other hand, in this method, isobutane of gasoline vapor-containing air from the fueling device 1 cannot be recovered, but desorbed butane of gasoline vapor-containing air is 4.2 L / min [30 L / min × (70 vol% −56 vol%)]. It can be recovered. In this way, this system can reduce the amount of low-boiling hydrocarbons such as butane and isobutane flowing into the adsorption tower, reduce the load on the adsorption tower, reduce the size of the adsorption tower, and switch adsorption / desorption. A longer time can be realized. Therefore, by adopting this method in the gasoline vapor recovery device 100, it becomes possible to recover low boiling point hydrocarbons such as butane and isobutane, and the gasoline recovery that is compact and can liquefy and condense the gasoline vapor efficiently. Device 100 can be obtained.

  As described above, the gasoline recovery apparatus 100 according to the first embodiment condenses the condensing device (second condensing pipe 20) that condenses the desorbed concentrated gasoline vapor-containing air and the gasoline vapor-containing air taken in from the fuel supply device 1. Since the condensing device (condenser tube 3) is provided separately, low-boiling hydrocarbons such as butane and isobutane that could not be recovered by the conventional method can also be efficiently recovered.

  Further, since the gasoline vapor recovery apparatus 100 can efficiently recover low-boiling hydrocarbons without decreasing the condensation temperature or increasing the compression pressure, the refrigerator 6 can be operated with high cooling efficiency. Furthermore, since the gasoline vapor recovery device 100 can reduce the power of the gasoline vapor compression pump 19, it can recover gasoline efficiently and efficiently without consuming unnecessary energy. In addition, since the gasoline vapor recovery apparatus 100 can efficiently liquefy low boiling point hydrocarbons, the amount of adsorbent used can be reduced, and the adsorption tower can be made compact.

  In the first embodiment, the second pressure controller 23 causes the pressure of the piping between the gasoline vapor compression pump 19 and the second pressure controller 23 to be provided at the subsequent stage of the adsorption / desorption tower 7 and the adsorption / desorption tower 8. Although the case where it is set to a value equivalent to 13 has been shown, the same effect can be obtained without providing the second pressure controller 23 if it can be set to an equivalent value. However, it is necessary to prevent the gasoline vapor-containing air flowing from the fuel filler 1 from flowing into the second condensing pipe 20 that condenses the gasoline component in the desorbed gas. When the second pressure controller 23 is provided, the set pressure of the second pressure controller 23 may be higher than the set pressure of the pressure controller 13. Thereby, the low boiling point hydrocarbons contained in the concentrated gasoline vapor can be recovered more efficiently.

  Furthermore, in the first embodiment, the case where the second heat medium storage tank 22 is provided, the heat medium is supplied to the second heat medium storage tank 22 by the liquid circulation pump 10, and the second condensing pipe 20 is cooled is shown. However, as shown in FIG. 2, a heat medium storage tank 31 capable of simultaneously cooling the condensing pipe 3 and the second condensing pipe 20 is provided, and the heat medium is circulated and supplied to the adsorption / desorption tower 7 and the adsorption / desorption tower 8. You may make it squeeze. Thereby, while being able to reduce a number of parts, the capacity | capacitance of the liquid circulation pump 10 can be made small. Therefore, the gasoline vapor recovery device 100 can reduce the amount of heat generated by the liquid circulation pump 10, and is inexpensive and consumes less energy.

Embodiment 2. FIG.
FIG. 3 is a schematic configuration diagram showing an overall configuration of a gasoline vapor recovery device 100a according to Embodiment 2 of the present invention. Based on FIG. 3, the structure of the gasoline vapor collection apparatus 100a and the flow of the gasoline vapor will be described. Similarly to the gasoline vapor recovery apparatus 100 according to the first embodiment, the gasoline vapor recovery apparatus 100a also recovers the gasoline vapor by cooling it with the condenser tube 3, and also uses two adsorption / desorption towers that adsorb or desorb the gasoline vapor. The function is appropriately switched to recover (adsorb) and reuse (desorb) gasoline vapor. In the second embodiment, differences from the first embodiment will be mainly described, and the same parts as those in the first embodiment are denoted by the same reference numerals.

  In the first embodiment, the case where the heat medium is cooled by the heat exchanger 5 and the refrigerator 6 and the condensing pipe 3 and the second condensing pipe 20 are cooled to the same temperature by the heat medium is shown as an example. . On the other hand, in the second embodiment, the second heat exchanger 32 and the second refrigerator 33 for cooling the heat medium are provided in the second heat medium storage tank (referred to as the second heat medium storage tank 22a), and the second condensation is performed. The case where the tube (hereinafter referred to as the second condensing tube 20a) is cooled and the second condensing tube 20a is cooled at a temperature lower than that of the condensing tube 3 is shown as an example.

  With such a configuration, there is an effect that low-boiling hydrocarbons such as butane and pentane can be efficiently liquefied in the second condensing pipe 20a. Since the concentrated gasoline vapor-containing air flowing through the second condensing pipe 20a does not contain moisture, the water in the gas freezes inside the second condensing pipe 20a, and the gas flow is delayed in the second condensing pipe 20a. There is nothing. Therefore, the gasoline vapor recovery apparatus 100a can efficiently recover low-boiling hydrocarbons contained in the desorbed concentrated gasoline vapor, and can be made more compact.

Embodiment 3 FIG.
FIG. 4 is a schematic configuration diagram showing an overall configuration of a gasoline vapor recovery device 100b according to Embodiment 3 of the present invention. Based on FIG. 4, the structure of the gasoline vapor collection apparatus 100b and the flow of the gasoline vapor will be described. Similarly to the gasoline vapor recovery apparatus 100 according to the first embodiment, the gasoline vapor recovery apparatus 100b also recovers the gasoline vapor by cooling it with the condensing pipe 3, and also uses two adsorption / desorption towers that adsorb or desorb the gasoline vapor. The function is appropriately switched to recover (adsorb) and reuse (desorb) gasoline vapor. In the third embodiment, differences from the first and second embodiments will be mainly described, and the same parts as those in the first and second embodiments are denoted by the same reference numerals.

  In the first embodiment and the second embodiment, a condensing device (second condensing pipe) that condenses the desorbed concentrated gasoline vapor-containing air and a condensing device (condensing pipe 3) that condenses the gasoline vapor-containing air taken in from the fueling device 1. ) And are provided separately as an example. On the other hand, the third embodiment is provided with a gas flow rate variable pump 41 that is a variable gas supply device that can change the gas flow rate of air containing gasoline vapor, and is taken in from the concentrated gasoline vapor desorbed from the desorption tower 8 and the fuel supply device 1. An example is shown in which the gas is condensed in the condensing pipe 3 after being mixed with gasoline vapor.

  The gasoline vapor recovery device 100b includes a gasoline vapor suction pump 2, a second condensing pipe, a second heat medium storage tank, a second heat exchanger, a second refrigerator, a gasoline vapor compression pump, and a second gas-liquid separator. In addition, the second pressure controller is not provided, and the purge gas discharge pipe 17 is connected between the valve B1 and the gas flow rate variable pump 41. The gas flow rate variable pump 41 can change the gas flow rate of the gasoline vapor-containing air taken in from the fueling device 1.

The operation of the gasoline vapor recovery device 100b will be described.
At the gas station, refueling is performed irregularly. For this reason, the gas flow rate variable pump 41 is driven in the large flow rate mode for a limited time during refueling, and the gasoline vapor near the nozzle (not shown) of the refueling device 1 is recovered. On the other hand, when refueling is not performed, the valve B1 is closed and the gas flow rate variable pump 41 is driven in the small flow rate mode. Thus, the concentrated gasoline vapor-containing air drawn out from the desorption tower 8 by the suction pump 11 is supplied to the condensing pipe 3 via the gas flow rate variable pump 41.

  That is, the gasoline vapor recovery apparatus 100b condenses only the desorbed concentrated gasoline vapor-containing air in the condenser pipe 3 while refueling is not performed. By doing so, the gasoline vapor recovery apparatus 100b can efficiently recover the low-boiling hydrocarbons in the desorbed concentrated gasoline vapor-containing air. Therefore, by performing the desorption operation for a long time, the gasoline components stored in the adsorption / desorption tower can be reduced, and the amount of gasoline that can be adsorbed in the next round can be increased.

  However, since the operation time of the suction pump 11 and the gas flow rate variable pump 41 is increased, the energy consumption is increased. For this reason, when the suction pump 11 is operated for a predetermined time, the suction pump 11 is preferably stopped, and the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are switched at that time. By doing so, the gasoline vapor-containing air discharged from the gas-liquid separator 9 to the adsorption / desorption tower where the gasoline component is not always adsorbed, except when the gasoline vapor is continuously supplied from the fueling device 1. This makes it possible to adsorb and remove gasoline vapor with high efficiency.

  That is, when the stop time of the fuel supply device 1 becomes longer than the operation time of the suction pump 11, low-boiling hydrocarbons that are not condensed in the condenser tube 3 are supplied to the adsorption / desorption tower (for example, the adsorption / desorption tower 7) in which no gasoline component remains. can do. Therefore, low-boiling point hydrocarbons can be efficiently adsorbed in the adsorption / desorption tower, and the amount of the adsorbent used in the adsorption / desorption tower can be reduced. From the above, the gasoline vapor recovery device 100b is inexpensive and compact. Note that either or both of the feature items of the first embodiment and the feature items of the second embodiment may be applied to the third embodiment.

Embodiment 4 FIG.
FIG. 5 is a schematic configuration diagram showing an overall configuration of a gasoline vapor recovery device 100c according to Embodiment 4 of the present invention. Based on FIG. 5, the structure of the gasoline vapor collection apparatus 100c and the flow of the gasoline vapor will be described. Similarly to the gasoline vapor recovery apparatus 100 according to the first embodiment, the gasoline vapor recovery apparatus 100c also recovers the gasoline vapor by cooling it with the condensing pipe 3, and also uses two adsorption / desorption towers that adsorb or desorb the gasoline vapor. The function is appropriately switched to recover (adsorb) and reuse (desorb) gasoline vapor. In the fourth embodiment, differences from the first to third embodiments will be mainly described, and the same parts as those in the first to third embodiments are denoted by the same reference numerals.

  In Embodiment 3, the case where the gas flow rate variable pump 41 which can change the gas flow rate of gasoline vapor containing air is shown as an example. On the other hand, in Embodiment 4, the gas outlet of the gas-liquid separator 9 is provided with a third heat exchanger 52 (refrigeration device) that is one of the components of the third refrigerator 51, and the third heat exchanger. The case where the gasoline vapor which flowed out from the gas-liquid separator 9 via 52 is cooled is shown as an example. In other words, the second condensing pipe, the second heat medium storage tank, the second heat exchanger, the second refrigerator, the gasoline vapor compression pump, the second gas-liquid separator, and the second pressure controller are not provided. This is the same as the gasoline vapor recovery apparatus 100b according to the second embodiment, but differs from the third embodiment in that the gasoline vapor suction pump 2 is used instead of the gas flow rate variable pump 41.

  With such a configuration, the gasoline vapor-containing air flowing out from the gas-liquid separator 9 can be cooled by the third heat exchanger 52. Thereby, the temperature of the gasoline vapor-containing air can be further lowered in the adsorption / desorption tower 7 and the adsorption / desorption tower 8. Therefore, the removal ability of low boiling point hydrocarbons in the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be increased. From the above, the gasoline vapor recovery apparatus 100c can liquefy gasoline vapor with high efficiency.

  In addition, by putting metal particles in the adsorption / desorption tower 7 and the adsorption / desorption tower 8 (also in the first to third embodiments and the fifth to seventh embodiments), the cooling performance of the adsorbent is increased. The adsorption / removal performance of low-boiling hydrocarbons can be further enhanced. The metal particles have good thermal conductivity, and aluminum or copper that is not corroded by gasoline vapor or the like is suitable. Further, any one or more of the feature items of the first embodiment to the feature items of the third embodiment may be applied to the fourth embodiment.

Embodiment 5 FIG.
FIG. 6 is a schematic configuration diagram showing an overall configuration of a gasoline vapor recovery device 100d according to Embodiment 5 of the present invention. Based on FIG. 6, the structure of the gasoline vapor collection apparatus 100d and the flow of the gasoline vapor will be described. Similarly to the gasoline vapor recovery apparatus 100 according to the first embodiment, the gasoline vapor recovery apparatus 100d also recovers the gasoline vapor by cooling it with the condensing pipe 3, and also uses two adsorption / desorption towers that adsorb or desorb the gasoline vapor. The function is appropriately switched to recover (adsorb) and reuse (desorb) gasoline vapor. In the fifth embodiment, differences from the first to fourth embodiments will be mainly described, and the same parts as those in the first to fourth embodiments are denoted by the same reference numerals.

  As shown in FIG. 6, the gasoline vapor recovery device 100 d is configured to connect the gas outlet of the gas-liquid separator 9 and the second condensing pipe 63, and to include a second gasoline vapor compression pump 61 that is a compression pump therebetween. Is. That is, the gasoline vapor recovery device 100d further compresses the gasoline vapor-containing air that has passed through the condensing pipe 3 and the gas-liquid separator 9 with the second gasoline vapor compression pump 61, and then supplies the compressed air to the second condensing pipe 63. It is a thing. The gasoline vapor-containing air recompressed by the second gasoline vapor compression pump 61 is supplied to the second condensing pipe 63 provided in the second heat medium storage tank 64, and the remaining low boiling point hydrocarbon is condensed. To do.

  The gasoline vapor-containing air from which the low-boiling hydrocarbons have been condensed and removed is supplied to the adsorption / desorption tower 7 or the adsorption / desorption tower 8 via the second gas-liquid separator 62. Since the ultimate pressure is the same as when the target pressure is set in one stage and when the target pressure is set in two stages, the amount of gasoline vapor supplied to the adsorption / desorption tower 7 or the adsorption / desorption tower 8 is different. Absent. However, in the case of two-stage compression, there is a gasoline component that is liquefied in the first stage, so the amount of gasoline vapor-containing air that must be compressed in the second stage is reduced, and it is used when compressing gasoline vapor-containing air. Energy can be reduced.

  In addition, by doing so, the gasoline vapor-containing air from which the low-boiling point hydrocarbons are condensed and removed is supplied to the adsorption / desorption tower 7 or the adsorption / desorption tower 8, and is thus removed by the adsorption / desorption tower 7 and the adsorption / desorption tower 8. Low boiling hydrocarbons that had to be reduced can be reduced. Therefore, the adsorbent filled in the adsorption / desorption tower 7 and the adsorption / desorption tower 8 can be reduced.

  From the above, the gasoline vapor recovery device 100d is provided with a plurality of condensing devices (a condensing device composed of the condensing tube 3 and a condensing device composed of the second condensing tube 63), and is compressed in two stages. While reducing the energy required for compressing the vapor-containing air, the low-boiling hydrocarbons can be liquefied and removed with high efficiency, and the gasoline vapor can be recovered with high efficiency and energy saving. Note that one or more of the feature items of the first embodiment to the feature items of the fourth embodiment may be applied to the fifth embodiment.

Embodiment 6 FIG.
FIG. 7 is a schematic configuration diagram showing an overall configuration of a gasoline vapor recovery device 100e according to Embodiment 6 of the present invention. Based on FIG. 7, the structure of the gasoline vapor collection apparatus 100e and the flow of the gasoline vapor will be described. Similarly to the gasoline vapor recovery apparatus 100 according to the first embodiment, the gasoline vapor recovery apparatus 100e also recovers the gasoline vapor by cooling it with the condensation pipe 3, and adsorbs or desorbs the gasoline vapor. These functions are appropriately switched to recover (adsorb) and reuse (desorb) gasoline vapor. In the sixth embodiment, differences from the first to fifth embodiments will be mainly described, and the same parts as those in the first to fifth embodiments are denoted by the same reference numerals.

  As shown in FIG. 7, the gasoline vapor recovery apparatus 100e is a second adsorption / desorption apparatus that adsorbs and removes low-boiling hydrocarbons in low-concentration gasoline vapor-containing air discharged from the adsorption / desorption tower 7 and the adsorption / desorption tower 8. A low-boiling hydrocarbon adsorption / desorption tower 71 and a low-boiling hydrocarbon adsorption / desorption tower 72 as a second adsorption / desorption apparatus are provided. That is, the gasoline vapor-containing air discharged from the adsorption / desorption tower 7 operating as an adsorption tower is supplied to the low-boiling hydrocarbon adsorption / desorption tower 71 operating as an adsorption tower, where low-boiling hydrocarbons are removed. And released into the atmosphere. As the adsorbent filled in the low-boiling hydrocarbon adsorption / desorption tower 71 and the low-boiling hydrocarbon adsorption / desorption tower 72, silica gel having a pore size of 5 to 10 angstroms, synthetic zeolite alone, or a mixture thereof is effective. is there. Thereby, low boiling point hydrocarbons can be adsorbed efficiently.

  The switching between the low-boiling hydrocarbon adsorption / desorption tower 71 and the low-boiling hydrocarbon adsorption / desorption tower 72 and the switching between the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are performed by the gasoline vapor suction pump 2 and the suction pump 11. The total operating time can be mentioned. That is, when these accumulated operating times reach a predetermined time, for example, there is a method of simultaneously switching between the adsorption / desorption tower 7 and the adsorption / desorption tower 8, the low-boiling hydrocarbon adsorption / desorption tower 71, and the low-boiling hydrocarbon adsorption / desorption tower 72. is there. For desorption, the adsorption / desorption tower 7, the adsorption / desorption tower 8, the adsorption / desorption tower 71 for low-boiling hydrocarbons, and the adsorption / desorption tower 72 for low-boiling hydrocarbons are desorbed in parallel in order to suppress re-adsorption as much as possible. Is more desirable than connecting and removing in series.

  Next, when adsorbing in the low-boiling point hydrocarbon adsorption / desorption tower 71 and the low-boiling point hydrocarbon adsorption / desorption tower 72 (when the adsorbing material for low-boiling point hydrocarbons is filled in the adsorption / desorption tower 7 and the adsorption / desorption tower 8) In addition to the adsorption / desorption tower 7 and the adsorption / desorption tower 8, the low-boiling hydrocarbon adsorption / desorption tower 71 and the low-boiling hydrocarbon adsorption / desorption tower 72 are used in combination. The gasoline vapor-containing air discharged from the condenser 3 and the gas-liquid separator 9 contains several tens of types of hydrocarbons. Therefore, in the low-boiling hydrocarbon adsorbent, molecules having a relatively small molecular diameter can be adsorbed, but large molecules cannot be adsorbed. Therefore, when the adsorption / desorption tower 71 for low boiling point hydrocarbons and the adsorption / desorption tower 72 for low boiling point hydrocarbons adsorb, the leakage of hydrocarbons having a large molecular diameter is accelerated.

  On the other hand, when the adsorption / desorption tower 71 for low boiling point hydrocarbons and the adsorption / desorption tower 72 for low boiling point hydrocarbons are used in combination with the adsorption / desorption tower 7 and the adsorption / desorption tower 8, hydrocarbons having a large molecular diameter are adsorbed / desorbed. 7 or the adsorption / desorption tower 8 is adsorbed and removed, and the hydrocarbon having a small molecular diameter is adsorbed and removed by the low-boiling hydrocarbon adsorption / desorption tower 71 or the low-boiling hydrocarbon adsorption / desorption tower 72. Therefore, hydrocarbons in gasoline vapor-containing air can be efficiently adsorbed and removed. From the above, the gasoline vapor recovery apparatus 100e can liquefy and remove low-boiling hydrocarbons with high efficiency by arranging adsorption / desorption towers with different adsorbents in series and performing two-stage adsorption, Gasoline vapor can be collected with high efficiency. Note that any one or more of the characteristic items of the first embodiment to the fifth embodiment may be applied to the sixth embodiment.

Embodiment 7 FIG.
FIG. 8 is a schematic configuration diagram showing an overall configuration of a gasoline vapor recovery device 100f according to Embodiment 7 of the present invention. Based on FIG. 8, the structure of the gasoline vapor collection apparatus 100f and the flow of the gasoline vapor will be described. Similarly to the gasoline vapor recovery apparatus 100 according to the first embodiment, the gasoline vapor recovery apparatus 100f also recovers the gasoline vapor by cooling it with the condensation pipe 3, and adsorbs or desorbs the gasoline vapor. These functions are appropriately switched to recover (adsorb) and reuse (desorb) gasoline vapor. In the seventh embodiment, differences from the first to sixth embodiments will be mainly described, and the same parts as those in the first to sixth embodiments are denoted by the same reference numerals.

  In the sixth embodiment, switching between the low-boiling hydrocarbon adsorption / desorption tower 71 and the low-boiling hydrocarbon adsorption / desorption tower 72 and switching between the adsorption / desorption tower 7 and the adsorption / desorption tower 8 are performed by the gasoline vapor suction pump 2 or the suction. The case where it performs simultaneously with the operation | movement integration time of the pump 11 was shown. On the other hand, in Embodiment 7, a gas flow rate variable pump 41 capable of changing the gas flow rate of gasoline vapor-containing air is provided, and the adsorption / desorption tower 7, the adsorption / desorption tower 8, the low-boiling hydrocarbon adsorption / desorption tower 71, and the low-boiling point. The hydrocarbon adsorption / desorption column 72 can be desorbed independently.

  By providing the gas flow rate variable pump 41, the gasoline components adsorbed in the adsorption / desorption tower 7, the adsorption / desorption tower 8, and the low-boiling hydrocarbon adsorption / desorption tower 71 and the low-boiling hydrocarbon adsorption / desorption tower 72 are independent. There is an effect that it can be detached and regenerated. Therefore, the gasoline vapor recovery device 100f can efficiently recover the low boiling point hydrocarbons contained in the desorbed concentrated gasoline vapor, and can be made compact. Note that any one or more of the characteristic items of the first embodiment to the sixth embodiment may be applied to the seventh embodiment.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 1 Oil supply apparatus, 2 Gasoline vapor suction pump, 3 Condensation pipe, 4 Heat medium storage tank, 5 Heat exchanger, 6 Refrigerator, 7 Adsorption / desorption tower, 8 Adsorption / desorption tower, 9 Gas-liquid separator, 10 Liquid circulation pump, 11 Suction pump, 12 Gasoline tank, 13 Pressure controller, 14 Gasoline vapor feed pipe, 15 Purified air discharge pipe, 16 Purge gas inflow pipe, 17 Purge gas exhaust pipe, 18 Gas-liquid mixed gasoline outflow pipe, 19 Gasoline vapor compression pump, 20 2 condensation pipe, 20a 2nd condensation pipe, 21 2nd gas-liquid separator, 22 2nd heat medium storage tank, 22a 2nd heat medium storage tank, 23 2nd pressure controller, 31 heat medium storage tank, 32 2nd heat Exchanger, 33 2nd refrigerator, 41 Gas flow variable pump, 51 3rd refrigerator, 52 3rd heat exchanger, 61 Gasoline vapor compression pump, 62 2 gas-liquid separator, 63 second condensing pipe, 64 second heat medium storage tank, 71 low boiling point hydrocarbon adsorption / desorption tower, 72 low boiling point hydrocarbon adsorption / desorption tower, 100 gasoline vapor recovery device, 100a gasoline vapor recovery Equipment, 100b Gasoline vapor recovery device, 100c Gasoline vapor recovery device, 100d Gasoline vapor recovery device, 100e Gasoline vapor recovery device, 100f Gasoline vapor recovery device, B1 valve, B2 valve, B3 Desorption valve, B4 Adsorption valve for adsorption, B5 Mass flow controller, B6 inflow valve for adsorption, B7 valve.

Claims (7)

A condenser for cooling the gasoline vapor;
A gas-liquid separator that is provided on the downstream side of the condensing device, and separates the gasoline liquid cooled and condensed into liquid by the condensing device and the non-liquefied gasoline vapor;
An adsorption / desorption device that is provided on the gas downstream side of the gas-liquid separator and adsorbs / desorbs the gasoline vapor separated by the gas-liquid separator;
A gasoline condenser connected to the adsorption / desorption device, supplied with the gasoline vapor desorbed by the adsorption / desorption device, and having a second condenser for cooling the gasoline vapor,
A heat medium storage tank for storing a heat medium for cooling the condensing device and the second condensing device;
The heat medium storage tank that stores the heat medium that cools the second condensing device in the heat medium storage tank, and the heat that stores the heat medium that cools the condensing device in the heat medium storage tank in the adsorption / desorption device. An apparatus for recovering gaseous hydrocarbons, wherein the heat medium in a medium storage tank is supplied in parallel . The gaseous hydrocarbon recovery device according to claim 1 , wherein the condensing device and the second condensing device are provided in a common or separate heat medium storage tank. Equipped with a refrigerator,
The apparatus for recovering gaseous hydrocarbons according to claim 1 or 2 , wherein the heat medium stored in the heat medium storage tank is cooled by a heat exchanger constituting the refrigerator. A pressure pump for pressurizing gasoline vapor supplied from the adsorption / desorption device is provided between the adsorption / desorption device and the second condensing device;
The gaseous hydrocarbon recovery device according to any one of claims 1 to 3 , wherein a pressure controller that adjusts the pressure in the second condensing device is provided downstream of the second condensing device. A method for recovering gaseous hydrocarbons using the gaseous hydrocarbon recovery device according to any one of claims 1 to 4 ,
Condensed gasoline vapor-containing air desorbed and desorbed during non-refueling time periods, and sucked gasoline vapor-containing air and desorbed concentrated gasoline vapor-containing air are mixed and treated during refueling time periods A method for recovering gaseous hydrocarbons. A method for recovering gaseous hydrocarbons using the gaseous hydrocarbon recovery device according to any one of claims 1 to 4 ,
Switching between the adsorption device and the desorption device of the adsorption / desorption device every predetermined time. A method for recovering gaseous hydrocarbons. The said predetermined time is set based on the integrated value of the operation time of the said gaseous hydrocarbon collection | recovery apparatus. The recovery method of the gaseous hydrocarbon of Claim 6 characterized by the above-mentioned.

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