JP2008093571A - Device for treating and recovering gaseous hydrocarbon and its method - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a small-sized and inexpensive device for treating and recovering hydrocarbons which concentratedly liquifies gasoline contained in a gasoline vapor in a certain portion and efficiently returns the liquified gasoline to an oiler. <P>SOLUTION: The device for treating the gasoline vapor leaked in the course of supplying gasoline is provided with a gasoline vapor supply means 2 for sucking and supplying the gasoline vapor generated in the vicinity of the supply part of a gasoline supply apparatus 1, a concentrating apparatus 3 for liquifying the gasoline vapor, a vapor-liquid separator 9 installed in the gas lowerstream side of a post stage and separating a gasoline liquid liquefied in the concentrating apparatus and the gasoline vapor, and an adsorbing and desorbing device 7, 8 for the gasoline vapor which is installed in the gas lowerstream side of the post stage. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to an apparatus and method for treating and recovering gaseous hydrocarbons contained in an atmospheric emission gas, and more particularly to an apparatus and method for treating gasoline vapor that leaks when gasoline is supplied.

In the conventional method for removing gaseous hydrocarbons by adsorbent / desorbent, the gas generated from the exhaust gas source (exhaust gas containing about 40 vol% gasoline vapor) is blower or self-pressure from the exhaust gas feed pipe to the adsorption tower. The exhaust gas that has been fed and finished the adsorption process is air (clean gas) containing 1 vol% or less of gasoline vapor from the top of the adsorption tower (adsorption tower after switching to the desorption process) through the exhaust pipe. ) Is released into the atmosphere.
In this case, the adsorption tower is operated while alternately switching the adsorption process and the desorption process described later, and this switching time (Swing Time) is set to about 5 minutes.

On the other hand, the purge gas is supplied to the adsorption tower after the adsorption step through the purge gas supply pipe, and desorption is performed by suction with a vacuum pump. A part of the clean gas discharged from the top of the adsorption tower during the adsorption operation is used as the purge gas, and the vacuum pump is operated at about 25 Torr.
The purged exhaust gas containing gasoline vapor after desorption is supplied to a gasoline recovery device through an air supply pipe and is brought into contact with liquid gasoline through a distribution pipe to recover the gasoline vapor in the purge exhaust gas as a liquid (gasoline absorbing liquid).

A slight amount of gasoline vapor remains in the exhaust gas from the gasoline collector, so it is returned to the exhaust gas pipe again through the return pipe, and adsorbed with the exhaust gas from the exhaust gas generation source. In order to cool the adsorbent layer in the adsorption tower, cooling water is circulated through the inner cylinder.
With this configuration, almost all of the gasoline vapor can be recovered as liquid gasoline, and the concentration of the gasoline vapor discharged from the adsorption tower is sufficiently low so that it does not cause air pollution (for example, patents) Reference 1).

Japanese Patent No. 2766793 (page 3-6, FIG. 1)

In the recovery method in which gasoline vapor is desorbed by the vacuum pump of Patent Document 1, the motive energy of the pump becomes extremely large, which is not realistic.
In addition, in order to perform a large amount of exhaust gas adsorption treatment, it is necessary to enlarge the adsorption tower or shorten the switching time between adsorption and desorption (Swing Time). However, the problem of the installation area and the problem of the cost of the adsorbent remain. In addition, if the switching time is shortened, the adsorbed gasoline vapor cannot be sufficiently desorbed, and the life of valves and the like is shortened.

Furthermore, the gasoline vapor-containing purge exhaust gas from which the adsorbed gasoline vapor is desorbed is brought into contact with liquid gasoline to recover the gasoline, and the gas is supplied again to the adsorption tower. Since the mist is supplied to the adsorption tower, there is a problem that the switching time of the adsorption tower is shortened.
In addition, since gasoline vapor is generated mainly during refueling, a fueling device is a source of gasoline vapor. In the conventional device, since the liquid gasoline was used for the recovered gasoline vapor, the recovered liquid gasoline and the liquid gasoline used for the recovery cannot be separated, and only the recovered gasoline vapor cannot be returned to the refueling device. There was a problem.

  The present invention has been made to solve the above-described problems, and is small in size that can liquefy gasoline contained in gasoline vapor intensively at a certain site and efficiently return the liquefied gasoline to a fueling device. An object of the present invention is to provide an inexpensive apparatus and method for treating and recovering gaseous hydrocarbons.

  The apparatus for treating and recovering gaseous hydrocarbons according to the present invention is a device for processing gasoline vapor that leaks during gasoline refueling, and is a gasoline vapor supply that sucks and supplies gasoline vapor generated in the vicinity of a fueling part of the gasoline refueling device. Means, a condensing device for liquefying gasoline vapor, a gas-liquid separator provided on the downstream side of the gas, separating the gasoline liquid liquefied by the condensing device and the gasoline vapor, and provided on the downstream side of the gas of the latter stage And a gasoline vapor adsorption / desorption device.

  In addition, a condensing device and a gasoline vapor sucking means for sucking gasoline vapor are connected to the condensing device, and a gasoline vapor heat insulating pipe for insulating and maintaining the temperature of the gasoline vapor heated to high pressure by compression is provided. .

  Further, the apparatus for treating and recovering gaseous hydrocarbons according to the present invention controls the position and temperature of the liquid level of liquefied gasoline so that gasoline droplets and re-evaporated gasoline vapor are separated into the gasoline vapor-containing air after separation. Is to prevent mixing.

  The method for treating and recovering gaseous hydrocarbons according to the present invention is the method for treating and recovering gaseous hydrocarbons by pressurizing and cooling the gasoline vapor, and pressurizing the gasoline vapor taken in by the gasoline vapor supply means. The process of compressing, the process of preventing the temperature drop of pressurized gasoline vapor by heat insulation or heating, the process of cooling and liquefying high temperature gasoline vapor with a condenser, and the process of separating liquefied gasoline and gasoline vapor is there.

This invention realizes a small and inexpensive gaseous hydrocarbon treatment / recovery device that can liquefy gasoline contained in gasoline vapor intensively at a certain site and efficiently return the liquefied gasoline to the fueling device. can do.
In addition, by insulating the piping connecting the condensing device that liquefies gasoline vapor and the gasoline vapor supplying means for supplying gasoline vapor to the condensing device, the gasoline vapor is not liquefied in the piping, and the condensing device is efficient. In addition, gasoline vapor can be liquefied and a highly efficient gasoline vapor recovery device can be realized. Further, it is possible to prevent liquefied gasoline from flowing into the gasoline vapor supply means and the like, and to prevent the gasoline vapor supply pump from malfunctioning, thereby realizing a safe gasoline vapor recovery device. Furthermore, since it is possible to prevent liquefaction of gasoline in the pipe, it is possible to realize an energy-saving gasoline vapor recovery device in which gasoline vapor flows through the pipe.
In addition, by controlling the position of the liquid level of the liquefied gasoline, it is possible to prevent gasoline droplets from being mixed into the gasoline vapor-containing air, thus preventing gasoline vapor from entering the adsorption tower by re-evaporation of the gasoline droplets. The capacity of the adsorption tower can be reduced, and the gasoline vapor recovery device can be made compact. In addition, by controlling the temperature of the liquefied gasoline, it is possible to prevent the re-evaporated gasoline vapor from being mixed into the gasoline vapor-containing air after separation, and to reduce the capacity of the adsorption tower. Compact size can be realized.
In addition, when the liquefied and recovered gasoline liquid is returned to the refueling device, the flow of gasoline vapor from the refueling device to the gas-liquid separator is prevented, so the capacity of the adsorption tower can be reduced, and the gasoline vapor recovery device is compact. Can be realized.

Embodiment 1.
FIG. 1 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to Embodiment 1 of the present invention.
In FIG. 1, 1 is a fueling device, 2 is a gasoline steam suction pump for sucking gasoline steam generated in the vicinity of a fueling part of the fueling device 1, and this is a gasoline steam supply means. 3 is a condensing device for liquefying gasoline vapor, 4 is a temperature medium tank for storing a temperature medium (brine liquid or the like) for cooling the condensing apparatus 3, 5 is a heat exchanger for cooling the temperature medium in the temperature medium tank 4, and 6 is Refrigerators 7 and 8 for supplying refrigerant to the heat exchanger 5 are adsorption / desorption towers filled with an adsorbent (silica gel, zeolite, etc.) that adsorbs and removes gasoline vapor in the gasoline vapor-containing air discharged from the condenser 1. FIG. 1 shows an example in which 7 operates as an adsorption tower and 8 operates as a desorption tower. 9 is a gas-liquid separator that separates the gasoline liquid and gasoline vapor liquefied by the condenser 3, and 10 is a liquid circulation pump that supplies the temperature medium cooled by the heat exchanger 5 to the adsorption / desorption towers 7, 8. 11 is a suction pump for sucking and desorbing gasoline vapor adsorbed by the adsorbent in the adsorption / desorption towers 7 and 8, 12 is a gasoline tank for temporarily storing the gas-liquid separated gasoline liquid, and a gas-liquid separator 9 for gaseous substances. Prevent inflow into 13 is a pressure controller for adjusting the pressure in the adsorption tower 7, 14 is a gasoline vapor feed pipe connecting the gas-liquid separator 9 and the adsorption / desorption towers 7, 8, and 15 is provided at the top of the adsorption / desorption towers 7, 8. A gasoline vapor discharge pipe to the atmosphere, 16 is a purge gas inflow pipe for sending a part of the clean gas discharged from the adsorption tower 7 or 8 to the atmosphere as a purge gas to the desorption tower 8 or 7, and 17 is a suction pump 11 is connected to the adsorption / desorption towers 7 and 8, and the purge gas discharge pipe 18 after desorption is connected to the gasoline vapor suction pump 2, which is a gasoline vapor supply means, and the condenser 3. This is a gasoline vapor insulated pipe that insulates and maintains the temperature of the pipe, for example, the pipe is surrounded by a heat insulating material or the like. Reference numeral 19 denotes a gas / liquid mixed gasoline outflow pipe connected to the condenser 3 and the gas / liquid separator 9.

  B1 is a valve that is opened in conjunction with the operation of the fueling device 1, B2 is a valve that is opened when the gasoline liquid recovered by the gas-liquid separator 9 is supplied to the gasoline tank 12, and B3 is in the middle of the gasoline vapor supply pipe 14. An adsorption inflow valve for the adsorption / desorption towers 7 and 8 provided, B4 is an adsorption discharge valve for the adsorption / desorption towers 7 and 8 provided in the middle of the gasoline vapor discharge pipe 15, and B5 is provided in the purge gas inflow pipe 16. A mass flow controller B 6 for controlling the gas amount is a desorption valve for the adsorption / desorption towers 7 and 8 provided in the purge gas discharge pipe 17.

  Next, the operation of the gaseous hydrocarbon treatment / recovery device of FIG. 1 will be described. When the fueling device 1 is operated, the valve B1 is opened, the gasoline vapor suction pump 2 is operated, and gasoline steam (about 40 vol% at normal temperature) in the vicinity of the fueling portion of the fueling device 1 is sucked, for example, 0.2-0. Compressed and compressed to about 4 MPa and sent to the condenser 3. Normally, the gasoline vapor saturation concentration decreases when the pressure is compressed, so that the gasoline can be liquefied more efficiently when the pressure is compressed. However, when recovering gasoline vapor at a gas amount of about 100 L / min, it is not practical to pressurize to 0.4 MPa or more because the capacity of the gasoline vapor suction pump 2 becomes very large. In this case, the gasoline vapor is heated from 50 ° C. to about 100 ° C. by the compression operation of the gasoline vapor suction pump 2 in the gasoline vapor heat insulation pipe 18. However, in the present invention, since the gasoline vapor heat insulation pipe 18 is insulated, the inside of the pipe is not cooled by outside air or the like, so that the gasoline vapor is not liquefied in the gasoline vapor heat insulation pipe 18. By doing in this way, since a gasoline liquid does not flow into the gasoline vapor heat insulation pipe 18, the pressure loss in the gasoline vapor heat insulation pipe 18 can be reduced, and the capacity of the gasoline vapor suction pump 2 can be reduced. The energy consumption of the gasoline vapor suction pump 2 can be reduced. In addition, when the supply of gasoline vapor is stopped, the gasoline liquid can be prevented from flowing back to the gasoline vapor suction pump 2, and a failure of the gasoline vapor suction pump 2 can be prevented. Further, it is not necessary to make a gasoline liquid drain port in the gasoline vapor insulation pipe 18, it is not necessary to collect the liquefied gasoline from a plurality of locations, the system can be simplified, and the control operation of the system can be simplified.

  When the refrigerant is supplied from the refrigerator 6 to the heat exchanger 5 in the temperature medium tank 4, the condensing device 3 provided in the temperature medium tank 4 is indirectly cooled through the temperature medium. Normally, the inside of the condenser 3 is kept at about 0 ° C. to 5 ° C., and the water contained in the gasoline and gas is partially condensed, and the gas / liquid separator 9 is mixed with the gasoline liquid and the gasoline vapor. Supplied. Since the gas-liquid separator 9 is also provided in the temperature medium tank 4, it is separated into gas (gasoline vapor) and liquid (gasoline liquid) under the condition that the gasoline vapor is condensed by the condenser 3. The liquid accumulates below the condenser 3, and the gas is supplied to the adsorption / desorption towers 7 and 8. At this time, by introducing gasoline vapor from above the condenser 3 and flowing downward, the liquefied gasoline and moisture are efficiently flowed downward by gravity and gas flow, and these liquefied products can be easily recovered. Become.

  By the way, under the conditions of the pressure of 0.3 MPa, the cooling temperature of 5 ° C., and the gas flow rate of 100 L / min, which are the operating conditions of the condensing device 3, the gasoline vapor concentration is about 10 vol%. As can be seen from the gasoline vapor saturation diagram, at a pressure of 0.3 MPa and a temperature of 5 ° C., the saturated gasoline vapor concentration is approximately 10 vol%. Under these conditions, the gasoline vapor concentration should theoretically be 10 vol% or less. There is no. Further, the gasoline vapor concentration at the outlet of the condensing device 3 can be reduced by lowering the temperature. However, if the set temperature is below the freezing point, the water contained in the gas freezes in the condensing device 3 and the problem of clogging of the piping occurs. Therefore, the set temperature of the condensing device 3 may be set to about 0 ° C. to 5 ° C. desirable.

When the refueling time reaches a certain 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 has elapsed, the valve B2 is closed, and the gasoline liquid is stored in the lower part of the gas-liquid separator 9. At this time, since the gasoline tank 12 is provided, the gasoline vapor is prevented from flowing into the gas-liquid separator 9, and the adsorption / desorption towers 7, 8 are adsorbed by the high concentration gasoline vapor flowing into the adsorption / desorption towers 7, 8. Shortening of breakthrough time (shortening of switching timing) is prevented. That is, 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 flows from bottom to top. As a result, the gasoline tank 12 has a structure in which gasoline vapor exists 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 high-concentration gasoline vapor is supplied to the adsorption / desorption towers 7 and 8. Can be prevented.
By doing so, the capacity of the adsorption / desorption towers 7 and 8 is reduced, the entire apparatus is made compact, the switching time of the adsorption / desorption towers 7 and 8 is lengthened, and the life of the valves is lengthened. There is an effect that can be lengthened.

In the gas-liquid separator 9, it is important to prevent gasoline droplets from being mixed into gasoline vapor. When gasoline droplets enter the gasoline vapor supply pipe 14, the gasoline droplets re-evaporate in the gasoline vapor supply pipe 14, and the adsorption / desorption towers 7, 8 due to the high concentration gasoline vapor flowing into the adsorption / desorption towers 7, 8. It is necessary to shorten the switching time. Possible causes of the generation of gasoline droplets include collision of the gasoline liquid with the inner wall surface of the gas-liquid separator 9 and rebound of the gasoline liquid to the gasoline liquid accumulated in the lower part. Therefore, the inner diameter of the pipe for introducing the gasoline vapor / gasoline liquid mixture into the gas-liquid separator 9 is gradually increased, and the inflow rate of the gasoline vapor / gasoline liquid mixture into the gas-liquid separator 9 can be made as slow as possible. It is effective. In order to prevent the generation of gasoline droplets due to the rebound of the gasoline liquid, the gasoline liquid level in the gas-liquid separator 9 should be kept as low as possible, or the liquid surface area should be kept as small as possible and collected in the lower part. It is effective to make the contact between the gasoline liquid separated and the separated gasoline liquid as small as possible. Furthermore, by setting the temperature of the gasoline vapor supply pipe 14 equal to the condensation temperature of the condensing device 3 (not shown), it is possible to prevent the gasoline liquid from re-evaporating even if liquid droplets are mixed. Good. In this case, in order to prevent the droplets from flowing into the adsorption / desorption towers 7 and 8, the position of the supply port to the adsorption / desorption towers 7 and 8 is made higher than the position of the discharge port of the gas-liquid separator 9. is required.
By doing so, the capacity of the adsorption / desorption towers 7 and 8 is reduced, the entire apparatus is made compact, the switching time of the adsorption / desorption towers 7 and 8 is lengthened, and the life of the valves is lengthened. There is an effect that can be lengthened.

  Subsequently, about 10 vol% of gasoline vapor that could not be processed by the condenser 3 is sent to the adsorption / desorption towers 7 and 8 for processing. FIG. 1 shows a case where 7 is operating as an adsorption tower and 8 is operating as a desorption tower. Accordingly, the valve B3 is open (black), B3 ′ (white) is closed, the valve B4 is open (black), and B4 ′ (white) is closed. After the adsorption treatment for an arbitrary time in the adsorption tower 7, it is used as a desorption tower. In this case, the valves B3 and B4 are closed and B3 ′ and B4 ′ are open. Further, when the desorption of gasoline is completed, it is used again as an adsorption tower, and this operation is repeated over time. Adsorption / desorption switching is controlled by switching the valves B3, B4, B3 ′, B4 ′ as described above.

  The gasoline vapor is sent to the adsorption tower 7 through the gasoline vapor feed pipe 14. Adsorbents that adsorb gasoline vapor are enclosed in the adsorption / desorption towers 7 and 8. Silica gel was used as the gasoline vapor adsorbent. In particular, silica gel or synthetic zeolite having a pore diameter of 4 to 100 angstroms or a mixture thereof is effective. When gasoline vapor passes through the adsorbent, the gasoline component is adsorbed and removed, and becomes clean air having a gasoline concentration of 1 vol% or less and is released to the atmosphere through the gasoline vapor discharge pipe 15. Further, a pressure controller 13 for controlling the pressure to a specified value is disposed in the discharge pipe 15 to the atmosphere so that the pressure in the adsorption tower 7 is maintained at the specified value. In the present embodiment, adsorption is performed using the high-pressure (about 0.3 MPa) exhaust gas of the condensing device 3, so that the adsorption capacity is greatly improved as compared with adsorption at normal pressure.

The adsorption / desorption towers 7 and 8 are always cooled to a constant temperature by the temperature medium supplied by the liquid circulation pump 10 regardless of the role of gasoline vapor adsorption / desorption. That is, the operation of the cooling system of the condenser 3 and the adsorption / desorption towers 7 and 8 is always controlled so as to be maintained at the set temperature. This is because the adsorbent filled in the adsorption / desorption towers 7 and 8 is cooled by heat transfer from the finned tube heat exchanger provided in the adsorption / desorption towers 7 and 8, so that a certain amount of cooling time is required. This is because it is indispensable and cannot handle instantaneous driving. Furthermore, the provision of the refrigerator 6 having a large cooling capacity so that it can be cooled in a short time adversely affects the facility cost and makes it impossible to provide an inexpensive gasoline recovery device. In addition, by lowering the temperature inside the adsorption tower 7, it is possible to increase the adsorption capacity and reduce the amount of adsorbent used. However, if the internal temperature of the adsorption tower 7 is made lower than the set temperature of the condenser 3, the water is condensed in the adsorption tower 7, and when it is below freezing, the temperature is set to almost the same as that of the condenser 3. Better to do.
From the above, the cooling system of the condenser 3 and the adsorption / desorption towers 7 and 8 is maintained at the set temperature, and the pressure system of the condenser 3 and the adsorption / desorption towers 7 and 8 is maintained at the set pressure. Thus, efficient gasoline recovery can be performed by always controlling the operation.

  Next, the gasoline vapor desorption process 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 valve B6 'is opened and B6 is closed. At the time of adsorption, the adsorption tower operates at a high pressure of 0.3 MPa, but at the time of desorption, the pressure is reduced to the atmospheric pressure or less by the suction pump 11, so that the gasoline adsorbed on the adsorbent is desorbed by this pressure difference. In FIG. 1, the desorbed gasoline vapor is returned to the condensing device 3, and after the gasoline is condensed and recovered again, it is returned to the adsorption tower 7 again. While repeating this operation, the entire amount of gasoline is condensed and recovered in the condensing device 3. At the time of desorption, the desorption speed can be increased by increasing the temperature inside the desorption tower 8, but by increasing the temperature, the energy consumption increases in the refrigerator and the heater, and the adsorption / desorption tower 7, Therefore, it is effective to perform desorption at the same temperature as at the time of adsorption without increasing the temperature at the time of desorption.

Since only the desorption method using the pressure difference due to the suction of the suction pump 11 is not very efficient, it is effective to introduce the purge gas from the outside. In the present 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 '. B5 and B5 ′ are mass flow controllers that control the flow rate of gas passing therethrough. In this case, the mass flow controller B5 ′ is in an open state and can flow a specified amount of gas, and the mass flow controller B5 is closed and the gas flows. There is no such thing. In the present embodiment, the amount of moisture in the gas is made sufficiently low in the pre-stage condensing device 3, so that the moisture contained in the purge gas hardly affects the adsorbent in the desorption tower 8.
As a result of the desorption test, it was found that when the purge gas flow rate was 15 to 25 L / min, the pressure in the adsorption tower could be 15 to 30 kPa, and gasoline vapor could be efficiently desorbed.

  At the gas station, refueling is performed irregularly. For this reason, from the viewpoint of reducing the amount of electric power used, the gasoline vapor suction pump 2 is operated for a limited time during refueling, and the gasoline vapor in the vicinity of the refueling portion of the refueling device 1 is recovered. Further, the suction pump 11 and the liquid circulation pump 10 are operated in accordance with the operation of the gasoline vapor suction pump 2. Therefore, the gasoline vapor condensing operation by the condensing device 3, the gasoline vapor adsorbing operation by the adsorption tower 7, and the gasoline vapor desorbing operation by the desorption tower 8 are intermittent operations. On the other hand, the cooling operation of the temperature medium by the refrigerator 6 operates regardless of the operation of the fuel supply device 1 and is controlled to be cooled to a certain temperature. By performing such system control, it is possible to reduce energy consumption when the fueling device 1 is not in operation, and to realize an energy saving gasoline vapor recovery device.

  By the way, since the operation | movement of the oil supply apparatus 1 is intermittent as shown above, when oil supply is completed, a collection | recovery apparatus will stop. In this case, the valves B1 to B6 are fully closed. Thereby, it is possible to prevent the gasoline adsorbed on the adsorbent due to the pressure drop of the adsorption tower 7 from being desorbed and released into the atmosphere. Further, since the liquid circulation pump 10 that circulates the temperature medium is stopped with the stop of the fuel supply device, the gasoline vapor is desorbed from the adsorbent in the adsorption tower 7 due to the temperature rise of the adsorption tower 7, and the adsorption / desorption tower 7, There is a possibility that the pressure in 8 will rise. For this reason, the valves B3 and B3 ′ provided at the lower part of the adsorption / desorption towers 7 and 8 are opened to move the gasoline vapor adsorbed at the lower part of the adsorption tower 7 to the lower part of the desorption tower 8 and By increasing the pressure and the pressure in the desorption tower 8, the increase in pressure may be reduced. Thereby, it is possible to prevent an increase in the pressure of the recovery device while reducing energy consumption in a state where the fuel supply device 1 is not in operation, and a safe gasoline vapor recovery device can be realized.

Embodiment 2.
FIG. 2 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 2 of the present invention.
The difference between the present embodiment and the first embodiment is that the installation position of the gasoline vapor suction pump 2 which is a gasoline vapor supply means for sucking gasoline vapor in the vicinity of the oil supply portion of the oil supply device 1 is higher than the uppermost portion of the condenser device 3. This is the point. That is, the discharge port of the gasoline vapor suction pump 2 is provided above the inlet of the condensing device 3. Thereby, even if the gasoline vapor pressurized and compressed by the gasoline vapor suction pump 2 is liquefied, it does not flow back to the gasoline vapor suction pump 2, so that the gasoline vapor heat insulation pipe 18 does not need to be insulated. However, if the heavy gasoline vapor suction pump 2 is provided at the top of the condensing device 3, the center of gravity of the recovery device becomes high, and stability at the time of installation of the recovery device is lost. In such a case, the stability of the recovery device can be secured by strengthening the housing of the recovery device.

Embodiment 3.
FIG. 3 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 3 of the present invention.
In the first embodiment, the insulated gasoline vapor insulated pipe 18 is used as a pipe for supplying gasoline vapor from the gasoline vapor suction pump 2 which is a gasoline vapor supply means to the condenser 3. Is a liquefaction rate of gasoline vapor in a pipe for supplying gasoline vapor from the gasoline vapor suction pump 2 to the condenser 3 by using the gasoline vapor heating pipe 21 provided with heating means such as a heater. . By raising the temperature of the gasoline vapor by 20 to 30 ° C. above the temperature increased by the pressure compression, the gasoline vapor can be removed from the saturation region and can be prevented from condensing in the pipe.
In addition, since there is a possibility that gasoline vapor will burn if heated excessively, it may be necessary to devise such as using a heating means that is not excessively heated, such as performing temperature control with high accuracy.

Embodiment 4.
FIG. 4 is an overall configuration diagram showing a flow of the gaseous hydrocarbon treatment / recovery device according to Embodiment 4 of the present invention.
In the present embodiment, a gasoline vapor heating hot gas pipe 31 using a hot gas of the refrigerator 6 as a heating means for a pipe for supplying gasoline vapor from the gasoline vapor suction pump 2 to the condenser 3 as a gasoline vapor supply means. However, even if it does in this way, although heating efficiency falls, it is not necessary to use new energy and it may be advantageous in terms of energy consumption. In particular, when the operation time of the refrigerator 6 is long, it is effective as heating energy.

Embodiment 5.
FIG. 5 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to Embodiment 5 of the present invention.
In the first embodiment, the condensing device 3 and the gas-liquid separator 9 are placed in the temperature medium tank 4, and the gasoline vapor is supplied to the adsorption / desorption towers 7 and 8 through the insulated or non-insulated gasoline vapor supply pipe 14. However, in the present embodiment, by putting the gasoline vapor supply pipe 14 into the second temperature medium tank 41, the gasoline droplets flowing from the gas-liquid separator 9 are discharged into the gasoline vapor supply pipe 14. Thus, the amount of gasoline vapor supplied to the adsorption / desorption towers 7 and 8 is reduced as much as possible.
FIG. 5 shows an example in which the gas-liquid separator 9 and the gasoline vapor supply pipe 14 are placed in the second temperature medium tank 41, but the condenser 3, the gas-liquid separator 9, and the gasoline vapor supply pipe 14 are connected. You may put in one temperature medium tank, and you may put the condensing apparatus 3, the gas-liquid separator 9, and the gasoline vapor | steam feed pipe 14 in a separate temperature medium tank, respectively. In this case, the liquid circulation pump 10 allows the temperature medium to flow evenly, and the condenser 3, the gas-liquid separator 9, the gasoline vapor feed pipe 14, and the adsorption / desorption towers 7 and 8 are cooled to substantially the same temperature. In some cases, it is necessary to devise such as.

Embodiment 6.
FIG. 6 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to Embodiment 6 of the present invention.
In the present embodiment, a mist separator 51 constituted by a filter or the like is disposed inside the gas-liquid separator 9, and gas-liquid separation is ensured by capturing gasoline droplets generated in the gas-liquid separator 9. The discharge of gasoline droplets from the vessel 9 to the adsorption / desorption device is reduced.
Since the mist separator 51 needs to be replaced, it is necessary to devise a structure that allows the gas-liquid separator 9 to be easily removed from the temperature medium tank 4.

Embodiment 7.
FIG. 7 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment / recovery device according to Embodiment 7 of the present invention.
The difference between the present embodiment and the first embodiment is that the liquid surface position is monitored using a liquid surface sensor 61 that senses the liquid surface position of the liquid gasoline in the gas-liquid separator 9. In response to the signal, the liquid level controller 62 opens and closes the valve B2. As a result, it is possible to reliably prevent the gasoline droplets generated by the gas-liquid separated gasoline liquid from flowing into the gasoline liquid stored in the gas-liquid separator 9 from being mixed into the gasoline vapor. 7 and 8 can be reduced in size to make the entire apparatus more compact, and the switch life of the adsorption / desorption towers 7 and 8 can be lengthened to increase the life of the valve.

It is a whole block diagram which shows the flow of the processing and collection | recovery apparatus of the gaseous hydrocarbon which concerns on Embodiment 1 of this invention. It is a whole block diagram which shows the flow of the processing and collection | recovery apparatus of the gaseous hydrocarbon which concerns on Embodiment 2 of this invention. It is a whole block diagram which shows the flow of the processing and collection | recovery apparatus of the gaseous hydrocarbon which concerns on Embodiment 3 of this invention. It is a whole block diagram which shows the flow of the processing and collection | recovery apparatus of the gaseous hydrocarbon which concerns on Embodiment 4 of this invention. It is a whole block diagram which shows the flow of the processing and collection | recovery apparatus of the gaseous hydrocarbon which concerns on Embodiment 5 of this invention. It is a whole block diagram which shows the flow of the processing and collection | recovery apparatus of the gaseous hydrocarbon which concerns on Embodiment 6 of this invention. It is a whole block diagram which shows the flow of the processing and collection | recovery apparatus of the gaseous hydrocarbon which concerns on Embodiment 7 of this invention.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 1 Refueling device, 2 Gasoline vapor | steam suction pump (gasoline vapor supply means), 3 Condensing device, 4 Temperature medium tank, 5 Heat exchanger, 6 Refrigerator, 7, 8 Adsorption / desorption tower, 9 Gas-liquid separator, 10 Liquid circulation Pump, 11 Suction pump, 12 Gasoline tank, 13 Pressure controller, 14 Gasoline vapor supply pipe, 15 Gasoline vapor discharge pipe, 16 Purge gas inflow pipe, 17 Purge gas exhaust pipe, 18 Gasoline vapor insulation pipe, 19 Gas-liquid mixed gasoline outflow pipe, 21 Gasoline steam heating pipe, 31 Gasoline steam heating hot gas pipe, 41 Second temperature medium tank, 51 Mist separator, 61 Liquid level sensor, 62 Liquid level controller, B1, B2, B3, B4, B5, B6 valves.

Claims (10)

In the processing and recovery equipment for gaseous hydrocarbons for processing gasoline vapor that leaks during gasoline refueling,
Gasoline vapor supply means for sucking and supplying gasoline vapor generated in the vicinity of the oil supply part of the gasoline refueling device, a condensing device for liquefying gasoline vapor, and a gasoline liquid liquefied by the condensing device provided on the downstream side of the gas A gas hydrocarbon treatment / recovery device, comprising a gas-liquid separator for separating the gasoline vapor and a gas vapor adsorption / desorption device provided downstream of the downstream gas.   The gaseous carbonization according to claim 1, wherein the temperature of the condensing device, the gas-liquid separator, and the adsorption / desorption device is controlled to substantially the same temperature using a temperature medium whose temperature is controlled by a refrigerator or a cooling device. Hydrogen processing and recovery equipment.   3. The apparatus for treating and collecting gaseous hydrocarbons according to claim 1, wherein the installation position of the gasoline vapor supply means is provided above the inlet of the condensing device.   It is characterized in that a condensing device and a gasoline vapor suction means for sucking gasoline vapor are connected to the condensing device, and a gasoline vapor heat insulation pipe for insulating and maintaining the temperature of the gasoline vapor heated to high pressure by compression is provided. The apparatus for treating and recovering gaseous hydrocarbons according to claim 1 or 2.   A condensing device and a gasoline vapor suction means for sucking gasoline vapor are connected to the condensing device, and a gasoline vapor heating pipe for heating the temperature of the gasoline vapor, which has been heated by pressurization and compression, is provided by a heating means. The apparatus for treating and recovering gaseous hydrocarbons according to claim 1 or 2.   The gasoline tank for preventing the inflow of gaseous substances to the gas-liquid separator is provided in a pipe for discharging the gasoline liquid separated by the gas-liquid separator from the gas-liquid separator. The apparatus for treating / recovering gaseous hydrocarbons according to any one of 5.   The gas according to any one of claims 1 to 6, further comprising a mist separator for preventing gasoline droplets generated in the gas-liquid separator from flowing into the adsorption / desorption device. -Like hydrocarbon treatment and recovery equipment.   In the method for processing and recovering gaseous hydrocarbons, which is recovered by pressurizing and cooling the gasoline vapor, the process of compressing and compressing the gasoline vapor taken in by the gasoline vapor supply means, the temperature of the pressurized gasoline vapor is lowered by heat insulation or heating A method for treating and recovering gaseous hydrocarbons, comprising: a step of preventing, a step of cooling and liquefying high-temperature gasoline vapor with a condenser, and a step of separating liquefied gasoline and gasoline vapor.   In the method for treating and recovering gaseous hydrocarbons, which is recovered by pressurizing and cooling gasoline vapor, the gas pressure in the gas-liquid separator is maintained and the temperature of the separated gasoline liquid is stored while being cooled, and then stored. A method for treating and recovering gaseous hydrocarbons, characterized in that the gasoline liquid is discharged from the gas-liquid separator using the gas pressure in the gas-liquid separator in accordance with the amount of gasoline liquid stored.   In the method for treating and recovering gaseous hydrocarbons, which is recovered by pressurizing and cooling gasoline vapor, when the gasoline liquid is discharged from the gas-liquid separator, it passes through the gasoline liquid layer provided in advance. A method for treating and recovering gaseous hydrocarbons.

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