KR100728451B1 - Processing and recovery device of hydrocarbon gas - Google Patents

Abstract

assignment

An apparatus and method for treating and recovering gaseous hydrocarbons, which are small and inexpensive, are prevented from being poisoned by the influence of moisture contained in gasoline vapors.

Resolution

A first condensing device 6 for removing water and gasoline vapor contained in the gasoline vapor, and a gas downstream of the rear end thereof; The gasoline vapor adsorption-desorption apparatuses 2 and 3 provided are provided, and gasoline steam is supplied to the first condensation apparatus 6 and the adsorption-and-desorption apparatus 2 at the time of lubrication, and it absorbs in synchronization with the operation | movement. The gasoline vapor is discharged from the desorption apparatus 3, and the desorption gas is returned to the condensation apparatus for processing.

Apparatus for the treatment and recovery of gaseous hydrocarbons

Description

PROCESSING AND RECOVERY DEVICE OF HYDROCARBON GAS}

BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a first embodiment of the present invention, showing an example in which one condenser is provided.

FIG. 2 is an overall configuration diagram showing a flow of a gaseous hydrocarbon processing and recovery apparatus according to a first embodiment of the present invention, showing an example in which a first condenser and a second condenser are provided. FIG.

3 is a perspective view showing a part of the internal structure of the adsorption-desorption tower of FIGS. 1 and 2;

4 is a characteristic diagram for explaining a method for controlling the amount of purge gas;

5 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a second embodiment of the present invention.

6 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a third embodiment of the present invention.

7 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fourth embodiment of the present invention.

8 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fifth embodiment of the present invention.

9 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a sixth embodiment of the present invention.

10 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a seventh embodiment of the present invention.

FIG. 11 is a diagram showing the layout of a gaseous hydrocarbon treatment and recovery apparatus of FIG. 10; FIG.

12 is a perspective view illustrating a part of the internal structure of the adsorption and detachment tower of FIG. 10;

13 is a characteristic diagram for explaining a method for controlling the amount of purge gas.

14 is a characteristic diagram for explaining the relationship between the desorption time, the pressure in the desorption tower and the exhaust gasoline concentration from the desorption tower;

15 is a characteristic diagram for explaining the relationship between the pressure in the adsorption-and-desorption tower, the discharge gas flow rate from the adsorption-and-desorption tower, the exhaust gasoline concentration from the adsorption-and-desorption tower, and the discharge gasoline vapor flow rate from the adsorption-and-desorption tower.

Fig. 16 is a characteristic diagram for explaining the relationship between the pressure in the adsorption-and-desorption tower and the gasoline recovery flow rate in the condensation unit.

Fig. 17 is a perspective view partially cut out and showing an internal structure of an adsorption and desorption tower of a gaseous hydrocarbon processing and recovery apparatus according to an eighth embodiment of the present invention.

Fig. 18 is a structural diagram showing a gas circulation blower and a pump in the gaseous hydrocarbon processing and recovery apparatus according to the ninth embodiment of the present invention.

19 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a tenth embodiment of the present invention.

20 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to an eleventh embodiment of the present invention.

Fig. 21 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a twelfth embodiment of the present invention.

Fig. 22 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a thirteenth embodiment of the present invention.

Fig. 23 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fourteenth embodiment of the present invention.

Fig. 24 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fourteenth embodiment of the present invention.

Fig. 25 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fifteenth embodiment of the present invention.

Fig. 26 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fifteenth embodiment of the present invention.

Fig. 27 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a sixteenth embodiment of the present invention.

Fig. 28 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a seventeenth embodiment of the present invention.

Fig. 29 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a seventeenth embodiment of the present invention.

30 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to an eighteenth embodiment of the present invention;

Fig. 31 is a perspective view partially cut out and showing an internal structure of an adsorption and desorption tower of a gaseous hydrocarbon treatment and recovery apparatus according to a nineteenth embodiment of the present invention.

32 is a cross-sectional view of the adsorption and desorption tower of FIG.

Fig. 33 is an overall configuration diagram showing an appearance of a gaseous hydrocarbon treatment and recovery apparatus according to a twentieth embodiment of the present invention.

34 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a twenty-first embodiment of the present invention;

Fig. 35 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a twenty-second embodiment of the present invention.

(Explanation of symbols for the main parts of the drawing)

1 Exhaust gas generation source (oil supply nozzle) 2, 3 adsorption-desorption tower

4: gas circulation blower (pump) 5: liquefied gasoline recoverer

6: first condenser 7: second condenser

8: pump 9: gas-liquid separator

11: exhaust gas exhaust pipe 12a, 12b: exhaust pipe

13a, 13b: purge gas sending

14a, 14b: purge gas delivery pipe after desorption

21 silica gel 22 fin tube heat exchanger

41: pressure gauge 120a, 120b: pressure controller

201: refrigerator 202: liquid circulation pump

203: heat exchanger 204: temperature medium tank

205: auxiliary temperature medium tank 211: ejector

212: gasoline concentration sensor 213: thermometer

214: pressure regulating valve 215: filter

216 temperature sensor 217 pressure sensor

218: gas line 219: dry air generator

220: gas reservoir 221: frame arrester,

301: air gap B13a, B13b: mass flow controller

B101a, B101b: rectifier valve B103a, B103b: constant pressure valve,

R1, R2, R3a, R4a, R3b, R4b: refrigerant entrance

R5, R6: hot gas entrance HI, H2: heater

Field of technology

The present invention relates to an apparatus and method for treating and recovering gaseous hydrocarbons contained in atmospheric emission gas, and more particularly, to an apparatus and method for treating gasoline vapor leaked during gasoline refueling.

Conventional technology

In the conventional method for removing gaseous hydrocarbons using an adsorbent and desorbent, gas (exhaust gas containing about 40 vol% of gasoline vapor) generated from an exhaust gas generator is blown to the adsorption tower by a blower or a self-exhaust pipe by an exhaust gas exhaust pipe. The treated exhaust gas which has completed the adsorption process is atmosphere as air (clean gas) containing 1 vol% or less of gasoline vapor through the discharge pipe from the head of the adsorption tower (after switching to the desorption process). There is one to let go.

In this case, the adsorption column is operated while alternately switching the adsorption process and the desorption process described later, but the switching time (swing time) is about 5 minutes.

On the other hand, the purge gas is sent to the adsorption tower after the adsorption step through the purge gas supply pipe, and desorbed by suction with a vacuum pump. As the purge gas, a part of the clean gas discharged from the head of the adsorption tower during the adsorption operation is used, and the vacuum pump is operated at about 25 Torr.

The gasoline vapor-containing purge exhaust gas after desorption is sent to the gasoline recoverer through an air supply pipe, and is brought into contact with liquid gasoline through a distribution pipe to recover gasoline vapor in the purge exhaust gas as a liquid (gasoline absorbent liquid).

Since some gasoline vapor remains in the exhaust gas from a gasoline recoverer, it returns to an exhaust gas pipe again via a conveyance pipe, performs an adsorption process similarly to the exhaust gas from an exhaust gas generating source, and performs in the adsorption tower. Cooling water is circulated in the inner cylinder for cooling the adsorbent layer.

By 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 lowered and can be at a level that does not cause air pollution (for example, Japan). See Patent No. 2766793 (pages 3 to 6, FIG. 1).

In the recovery method of desorbing gasoline vapor with the vacuum pump of Japanese Patent No. 2766793, the power energy of the pump becomes very large and is not practical.

In addition, in order to adsorb a large amount of exhaust gas, it is necessary to increase the adsorption tower or shorten the swing time of adsorption and desorption. However, in the case of using a large adsorption tower, there is a problem of the installation area and the adsorbent. The problem of cost remains. In addition, if the switching time is shortened, there is a problem that the adsorbed gasoline vapor cannot be sufficiently desorbed, or the life of the valve or the like is shortened.

In addition, the gasoline vapor always contains water in the air. In the conventional system, since this water is also adsorbed simultaneously with the gasoline vapor, there is a problem that the adsorption performance of the adsorbent is lowered.

In addition, when used for recovery of gasoline vapor leaked at the time of refueling, gasoline vapor does not generate | occur | produce only at the time of refueling, and the frequency of occurrence varies with day or time and is not constant. Even in such a case, in the conventional apparatus, since adsorption and desorption are switched at regular intervals, gasoline vapor does not flow at all when it is hardly lubricated, such as on a weekday night. There is a problem that waste occurs.

SUMMARY OF THE INVENTION The present invention has been made to solve the above-described problems. The present invention prevents poisoning of the adsorbent under the influence of moisture contained in gasoline vapor, and furthermore, an apparatus and method for treating and recovering compact and inexpensive gaseous hydrocarbons. It is intended to provide.

Means to solve the problem

A gaseous hydrocarbon processing and recovery apparatus according to the present invention includes a condensation apparatus for removing water and gasoline vapor and a gasoline vapor adsorption and desorption apparatus provided on the gas downstream side of the condensation apparatus.

Moreover, the gas-hydrocarbon processing / recovery method which concerns on this invention WHEREIN: The adsorption-and-desorption apparatus which has an adsorption tower and a desorption tower by at least 1 tower, WHEREIN: It has a means to cool this adsorption-and-desorption apparatus, and it is a hole diameter of 4-100 as an adsorbent. The adsorption-desorption at low temperature is carried out using an angstrom silica gel or a synthetic zeolite alone or a mixture thereof, and a part of the outlet gas of the adsorption tower is sent to the desorption tower so that the gas at the time of desorption is used as the purge gas.

According to the present invention, the exhaust gas can be extremely clean (gasoline concentration of 1 vol% or less) by providing a condensation device for removing water and gasoline vapor and a gas adsorption and desorption device, and furthermore, a compact and inexpensive gasoline vapor. A recovery device can be realized. In particular, even when gasoline vapor contains water, the adsorbent may not be poisoned with water and freezing does not occur in the piping of the condenser or the adsorption and desorption device, thereby achieving stable operation. .

In addition, by controlling the temperature of the heat medium to a constant temperature and controlling the temperature of the condensation device and the adsorption and desorption device, the control circuit can be simplified and the cost can be reduced as compared with the case of individually controlling each device. Can be. In addition, since the temperature of the adsorption tower is made constant irrespective of adsorption and desorption, the energy required to cool the adsorption tower can be reduced, and an energy-saving gasoline vapor recovery device can be realized. In addition, since the adsorption tower is cooled, a large amount of gasoline vapor can be adsorbed with a very small amount of adsorbent, and the amount of the adsorbent used can also be reduced.

In addition, it is possible to suppress an abnormal temperature rise in the adsorption column due to the heat of adsorption, thereby making it possible to uniformize the temperature in the adsorption device and to ensure the safety of the adsorption device.

[First embodiment]

1 and 2 are overall configuration diagrams showing a flow of a gaseous hydrocarbon processing and recovery apparatus according to a first embodiment of the present invention, in which FIG. 1 is an example in which one condensing apparatus is provided, and FIG. The example which provided the condensation apparatus and the 2nd condensation apparatus is shown. 3 is a perspective view partially cut out of the internal structure of the adsorption and desorption tower of FIGS. 1 and 2, and FIG. 4 is a characteristic diagram for describing a method of controlling a purge gas flow rate.

1 and 2, 1 is an oil supply nozzle which is an exhaust gas generating source, 8 is a pump for sucking gasoline vapor from the oil supply nozzle 1, 6 is a first condensing device (first condensing device in FIG. 2), 7 is a 2nd condensation apparatus, 9 is a gas-liquid separator, 5 is a liquefied gasoline recovery machine, 2 and 3 are adsorption-and-desorption towers which are adsorption-and-desorption apparatus, and 4 is a gas circulation blower (pump). B1 is a valve which is closed except when lubrication of the oil supply nozzle 1, 11 is the 1st condenser 6 or the 1st, 2nd condenser 6, 7 and the adsorption-and-desorption tower 2, 3 The gasoline steam pipes to be connected, B11a and B11b, are adsorption valves for the adsorption and desorption towers 2 and 3 provided in the middle of the gasoline steam pipe 11, and 12a and 12b are heads of the adsorption and desorption towers 2 and 3. The discharge pipes 120a and 120b to the atmosphere provided in the air are pressure controllers disposed in the discharge pipes 12a and 12b.

Further, 13a and 13b are purge gas exhaust pipes for sending a part of the clean gas discharged from the adsorption tower 2 or 3 to the atmosphere as the purge gas to the desorption tower 3 or 2, and B13a and B13b are the purge gas transmissions. The mass flow controller 14a, 14b for controlling the amount of gas provided in the engines 13a, 13b is a desorption purge gas exhaust pipe connecting the gas circulation blower 4 and the adsorption and desorption towers 2, 3, and B14a, B14b are the same. It is a desorption valve of the adsorption-and-desorption towers 2 and 3 provided in the purge gas pipes 14a and 14b. R1 and R2 are inlets and outlets of refrigerant entering and exiting the first condenser 6, and R3 and R4 are inlets and outlets of lower temperature refrigerant entering and exiting the second condenser 7, R3a, R4a and R3b. , R4b is an inlet and an outlet of the low-temperature refrigerant entering and exiting the adsorption and desorption towers 2 and 3, respectively, and 41 is a pressure gauge provided on the exhaust side of the gas circulation blower 4.

Next, the operation of the gaseous hydrocarbon treatment and recovery apparatus of FIG. 1 will be described. When refueling is started at the gasoline stand, the pump 8 is operated to suck the gasoline vapor leaked from the refueling nozzle 1 (about 40 vol% at room temperature), and pressurized to about 0.3 MPa, for example, to condense the first condensation. Is sent to the device (6). The inside of the first condenser 6 is maintained at about 5 ° C by introducing a refrigerant from the inlet R1 and circulating it to the outlet R2, and the water contained in the gasoline and gas is partially condensed, and the gas liquid (Iii) separated into gas (gasoline vapor) and liquid (gasoline) through the separator (9), the liquid is stored below the first condensing device (6), and recovered as a liquid in the liquefied gasoline recoverer (5) The gas is discharged from the first condensation device 6. By introducing gasoline vapor from above the first condenser 6 and circulating downward, the liquefied gasoline and water flow down efficiently by gravity and gas flow, and the recovery of these liquefied liquids becomes easy.

By the way, the gasoline vapor concentration is about 10 vol% under the operating conditions of the first condensing device 6, 0.3 MPa, and 5 ° C. Subsequently, there may be a case where the lead is led to the adsorption and desorption towers 2 and 3, and as shown in FIG. 2, the lead is led to the second condensation device 7 again. This case is as follows.

Subsequently, about 10 vol% of gasoline vapor which has not been processed in the first condensation device 6 is sent to the second condensation device 7 for processing. The second condenser 7 is further introduced into the second condenser 7 by introducing a refrigerant having a lower temperature than the first condenser 6 from the inlet R3 and flowing it toward the outlet R4. It is set at a low temperature, for example, about -10 ° C. In the second condenser 7, gasoline and water are condensed and recovered similarly to the first condenser 6. Since the second condensation device 7 may operate at a temperature below the freezing point, in some cases, the gas in the second condensation device 7 is caused by ice generated in the second condensation device 7. There is a fear that the passage is blocked. In order to avoid this problem, it is effective to put in a process of melting ice (defrost) by stopping the circulation of the refrigerant at a predetermined time or circulating a high-temperature refrigerant. Moreover, you may arrange | position the apparatus (not shown) which can measure the pressure loss in the 2nd condensation apparatus 7, and if a pressure loss exceeds a set value, the sequence which introduces a defrost process may be prepared. Of course, you may form the sequence which detects a freezing state using another means which can detect the freezing state of the 2nd condensation apparatus 7, and moves to a defrost process when ice generate | occur | produces.

The gasoline vapor concentration is about 5 vol% under the operating conditions of the second condenser 7, 0.3 MPa and -10 ° C. The gasoline vapor is passed through the adsorption and desorption towers 2 and 3 for treatment. 1 and 2 show a case where the divalent adsorption tower and 3 operate as the desorption tower. Therefore, the valve B11a is in an open state, and the valve B11b is in a closed state. After the adsorption treatment at any time in the adsorption tower 2, it is used as a desorption tower. In this case, the valve B11a is closed and the valve B11b is used in an open state. In addition, when desorption of gasoline is complete | finished, it uses as an adsorption tower again, and this operation is used repeatedly over time. Switching of adsorption and desorption is controlled by switching of the valves B11a and B11b as described above.

The gasoline vapor is sent to the adsorption tower 2 through the exhaust pipe 11. The adsorption-and-desorption towers 2 and 3 are sealed with an adsorbent for adsorbing gasoline vapor. Silica gel was used as an adsorbent of gasoline vapor. Particularly effective are silica gels or synthetic zeolites having a pore size of 4 to 100 angstroms or mixtures thereof. As the gasoline vapor passes through the adsorbent, the gasoline component is adsorbed and removed, and becomes clean air with a gasoline concentration of 1 vol% or less, and is discharged to the atmosphere through the discharge pipe 12a. The adsorption tower 2 is cooled by a low temperature refrigerant or another method by using the second condensation device 7, and is intended to remove heat generated in the adsorption and increase the adsorption capacity. In addition, the adsorption capacity can be increased by lowering the temperature inside the adsorption tower 2.

However, if the internal temperature of the adsorption tower 2 is lower than the set temperature of the first condenser 6 or the second condenser 7, the water condenses in the adsorption tower 2, so that the first condensation In the case of the apparatus 6 only, it is better to set it to the temperature substantially the same as the 1st condensation apparatus 6. In addition, when the 2nd condensation apparatus 7 exists, it is better to set to the set temperature of the 2nd condensation apparatus 7. In addition, pressure controllers 120a and 120b for controlling the pressure to a prescribed value are disposed in the discharge pipes 12a and 12b to the atmosphere, and the pressure in the adsorption tower 2 is maintained at the prescribed value. In the case of FIG. 2, since the adsorption is performed by using the exhaust gas of the high pressure (about 0.3 MPa) of the second condensation apparatus 7, the adsorption capacity is significantly improved than the adsorption at normal pressure.

As shown in FIG. 3, the internal structure of the adsorption-and-desorption tower (2, 3) is a fin tube heat exchanger (refrigerant to the heat transfer tube with aluminum fins in consideration of heat transfer to the silica gel 21 or synthetic zeolite or a mixture thereof). And a silica gel 21, a synthetic zeolite, or a mixture thereof between the aluminum fins, and a rectifying plate 23 is provided up and down to improve gas flow. In this case, it is effective to fill the vent portion of the fin tube heat exchanger 22 with a fluorine-based filler so that gasoline vapor flows only between the aluminum fins and can be adsorbed efficiently. In addition, a lid may be provided to seal the space of the vent portion so that gasoline vapor does not flow into the space of the vent portion. In addition, 24 is a case, 25a, 25b are upper and lower flanges, and 26a, 26b are the outflow prevention nets of the silica gel 21.

When the first condenser 6 or the first and second condensers 6 and 7 are not provided in front of the adsorption and desorption towers 2 and 3, moisture contained in the gasoline vapor is adsorbed to the adsorbent. As a result, the adsorption performance of gasoline vapor is inferior, and an adsorbent in an amount more than necessary is required. In addition, when the temperature of the adsorption tower 2 is lowered below the freezing point, large troubles may occur such as water condensation on the surface of the adsorbent and clogging of the gas. In this embodiment, since the 1st condensation apparatus 6 or the 1st, 2nd condensation apparatus 6 and 7 was provided in front of the adsorption-and-desorption towers 2 and 3, moisture is also removed with gasoline vapor. Therefore, the adverse effect of the moisture in the adsorption-desorption towers 2 and 3 can be prevented beforehand. Moreover, the quantity of gasoline processed by the adsorption-and-desorption towers 2 and 3 can be significantly reduced, and the adsorption-and-desorption tower can be made small and inexpensive.

In this embodiment, when the 1st, 2nd condensation apparatus 6, 7 is provided, the 1st, 2nd condensation apparatus 6, the high concentration (40vol%) gasoline collect | recovered from the oil supply nozzle 1 is carried out. Since the volume can be reduced to 5 vol% in 7), the amount of gasoline treated by the adsorption and desorption towers 2 and 3 can be reduced to 12.5% (= 5% / 40%) relative to the total suction amount. That is, the volume of the adsorption-and-desorption towers 2 and 3 can be approximately 1/10 by providing the first and second condensation devices 6 and 7 at the front end of the adsorption-and-desorption towers 2 and 3. . In addition, as shown in FIG. 1, in the case of the first condenser 6 alone, the volume can be reduced to 10 vol%, and the amount of gasoline treated by the adsorption and desorption towers 2 and 3 is 25% (= 10% /) with respect to the total suction amount. 40%) can be reduced. In this case, the volumes of the adsorption-and-desorption towers 2 and 3 can be approximately 1/4.

Next, the desorption process will be described. When the gasoline adsorbed to the adsorbent is desorbed, the gas circulation blower 4 passes through the purge gas supply pipe 14a after desorption from the desorption tower 3 to suck gas into and desorb the gasoline from the adsorbent. At this time, the valve B14a is open and the valve B14b is closed. At the time of adsorption, the adsorption column operates at a high pressure of 0.3 MPa. However, at the time of desorption, the gas circulation blower 4 decompresses the pressure below atmospheric pressure. Thus, gasoline adsorbed to the adsorbent is desorbed by this pressure difference. In the case of FIG. 1, the desorbed gasoline vapor returns to the 1st condensation apparatus 6, and after condensing and recovering gasoline powder again, it returns to the adsorption-and-desorption towers 2 and 3 again. While repeating this operation, the entire amount of gasoline is condensed and recovered in the first condensation device 6. In the case of FIG. 2, the gas is returned to the second condensation device 7, and the gasoline powder is condensed and recovered again, and then returned to the adsorption and desorption towers 2 and 3 again. While repeating this operation, the entire amount of gasoline is condensed and recovered in the second condensation device 7.

If only the desorption method using the pressure difference by suction of the gas circulation blower 4, since the efficiency is not so high, it is effective to introduce purge gas from the outside. In this embodiment, a part of the clean gas discharged | emitted from the adsorption tower 2 to the atmosphere as this purge gas is sent to the desorption tower 3 by the discharge pipe 12a and the purge gas sending pipe 13a. B13a and B13b are mass flow controllers for controlling the flow rate of gas passing therein. In this case, the mass flow controller B13a is in a state capable of flowing a prescribed amount of gas in an open state, and the mass flow controller B13b is closed. As a result, gas does not flow. In the case where the gas flow rate is set to a constant gas flow rate, the rectifier valve may be used.

Further, as a result of the desorption test, it was found that when the purge gas flow rate was set to 15 to 25 L / min, the gasoline vapor could be efficiently desorbed by setting the pressure in the adsorption tower to 100 to 300 Torr.

As shown in Fig. 4A, the purge gas flow rate may be controlled to be constant at the time of desorption of gasoline vapor, but as shown in Fig. 4B, the purge gas flow rate varies with time.變) is more effective. That is, it is effective to increase the purge gas flow rate with the desorption time. Since there is also a large amount of gasoline vapor immediately after the start of desorption, a large amount of purge gas is not necessary, but the amount of gasoline desorbed with time decreases, so that the amount of suction gas also decreases. For this reason, it is effective to increase the purge gas flow rate and to prevent a decrease in the amount of suction gas. Since supplying unnecessary gas into the system leads to energy loss such as power of the gas circulation blower 4, it is preferable to suppress the purge gas flow rate to the minimum necessary. In addition, in this embodiment, the 1st condensation apparatus 6 or the 1st, 2nd condensing apparatus 6 and 7 of the front end of the adsorption-and-desorption towers 2 and 3 are made low enough the moisture content in gas. Therefore, the moisture contained in the purge gas hardly adversely affects the adsorbent in the desorption tower 3.

In addition, in this embodiment, although the temperature at the time of desorption of gasoline vapor is not changed to the setting temperature at the time of adsorption | suction, desorption is carried out by substitution by pressure change and the amount of purge gas, In order to further improve desorption efficiency, The flow of the coolant flowing from the inlet R3b to the outlet R4b in the desorption tower 3 may be temporarily stopped, and the temperature in the desorption tower 3 may be close to room temperature. By making the temperature at the time of desorption higher than the temperature at the time of adsorption, more efficient desorption can be implement | achieved. In the initial stage of desorption and transfer to the adsorption process, the temperature of the adsorption tower is high and the adsorption performance is low, but there is no risk of gasoline leakage because no gasoline remains in the adsorbent. As time passes, the amount of gasoline adsorption increases, but at the same time the temperature of the adsorption tower decreases and the adsorption performance of the adsorbent is improved. Therefore, rapid tower cooling is not necessary when transferring from desorption to the adsorption process. Of course, it is also possible to improve the desorption performance by forcibly heating the desorption tower 3 at the time of desorption. However, the energy consumption of the refrigerator and the heater is increased by shaking the temperature, which is inferior to the method of making the temperature at the time of energy absorption and desorption constant.

In a gasoline stand, refueling is done irregularly. For this reason, in the case of FIG. 2, the pump 8 is operated only for the limited time at the time of oil supply from a viewpoint of electric power consumption reduction, and the gasoline vapor which leaks from the oil supply nozzle 1 is collect | recovered. Therefore, the pump 8 and the first condensation device 6 become intermittent operation. On the other hand, the system including the closed loop circuit by the gas circulation blower 4, that is, the system including the second condensation device 7 and the adsorption-and-desorption towers 2 and 3, adopts a configuration of continuously operating. When circulating the gas in this closed loop circuit, there is a risk of inhaling the atmosphere from the gasoline oil supply nozzle 1, so that the valve B4 is inserted immediately before the gas circulation blower 4, and the pump ( It is effective to close the valve B4 when 8) is stopped and to open the valve B4 when the pump 8 is operating. By adopting such a structure, it is easy to keep the pressure in the adsorption tower 2 constant all the time, and the stable operation of the system becomes easy.

By the way, when lubrication is hardly performed, such as on a nighttime on a weekday, since no new gas is supplied in the closed circuit, the gas pressure may gradually decrease unless the pressure controllers 120a and 120b are disposed. . In this case, the gasoline adsorbed to the adsorbent may be desorbed and released into the atmosphere due to the pressure drop of the adsorption tower 2. In addition, there is a fear that a part of the pressure in the closed circuit excessively rises above the safety standard, and is accompanied by the risk of ignition. For this reason, in the case of FIG. 2, the pressure gauge 41 is arrange | positioned at the exhaust side of the gas circulation blower 4, and when it exceeds the prescribed | prescribed pressure range, the gas circulation blower 4 is stopped automatically. Safety measures are in place.

Second Embodiment

5 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a second embodiment of the present invention.

The difference from the 1st embodiment of this embodiment is the point which conveys the gasoline vapor desorbed from the desorption tower 3 to the 1st condensation apparatus 6 using the pump 8. In this embodiment, the gas circulation blower 4 used in FIG. 1 becomes unnecessary. However, if the pump 8 is intermittently operated only at the time of oil supply, the pressure of the adsorption-and-desorption towers 2 and 3 may change depending on the operation state of the pump 8, and it may be difficult to control the adsorption. In such a case, the valve B8 is inserted between the oil supply nozzle 1 and the pump 8, the pump 8 is always in operation, and the valve B8 is opened only when oil is being supplied. The system can be started.

[Third Embodiment]

6 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a third embodiment of the present invention.

In the first embodiment, a part of the outlet gas of the adsorption tower 2 is used as the purge gas at the time of desorption of the gasoline vapor. In the present embodiment, the desorption efficiency is improved by using outdoor air having a high temperature as the purge gas. It is an improvement. The valves B15a and B15b may be disposed in the purge gas air supply pipes 13a and 13b serving as the introduction ports of the outside air, and the amount of purge gas may be controlled by opening and closing the valves B15a and B15b. As described above, of course, a predetermined amount of purge gas may be supplied at the time of desorption of gasoline vapor, or the supply gas amount may be varied in time. In the case of using the outside air as the purge gas, the water contained in the outside air may be absorbed by the adsorbent in the desorption tower 3, so that the use such as the use in a situation where the humidity is not high or after dehumidification is effective is also effective. have.

Fourth Embodiment

7 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fourth embodiment of the present invention.

Although this embodiment is made to desorb gasoline vapor without using purge gas, although desorption efficiency falls even in this way, it may be simple and advantageous as a system. In particular, when the purge gas is not used, it is necessary to set the pressure difference and the temperature difference at the time of adsorption-desorption by setting the adsorption conditions to lower temperature and higher pressure and the desorption conditions to high temperature and low pressure.

[Fifth Embodiment]

8 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fifth embodiment of the present invention.

In this embodiment, hot gas flows from the inlet R5 to the outlet R6 instead of the refrigerant in the desorption tower 3 to raise the temperature in the desorption tower 3 to room temperature or more to improve desorption efficiency.

[Sixth Embodiment]

9 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a sixth embodiment of the present invention.

In this embodiment, the heaters H1a and H1b are disposed in the purge gas exhaust pipes 13a and 13b to improve the desorption performance by heating the purge gas.

[Seventh Embodiment]

10 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a seventh embodiment of the present invention.

The difference between the present embodiment and the first embodiment is that the temperature medium (such as brine solution) is cooled by using the refrigerator 201, and the temperature medium is first condensed by the liquid circulation pump 202. And it is a point to supply to the adsorption-and-desorption tower (2, 3). In other words, the temperature medium accumulated in the temperature medium tank 204 provided with the heat exchanger 203 is cooled by flowing a refrigerant from the freezer 201 to the heat exchanger 203, and the cooled temperature medium is a liquid. By the circulation pump 202, it supplies to the 1st condensation apparatus 6 and the adsorption-and-desorption towers 2 and 3. The temperature control of the temperature medium is performed by measuring the temperature of the temperature medium in the temperature medium tank 204 and controlling the operation of the refrigerator 201. In addition, in FIG. 10, the 1st condensation apparatus 6 is arrange | positioned in the temperature medium tank 204, and the example which made it supply to the adsorption-and-desorption towers 2 and 3 by the liquid circulation pump 202 is shown. .

In the figure, 1 is a fuel supply nozzle which is an exhaust gas generation source, 8 is a pump for sucking gasoline vapor from the fuel supply nozzle 1, 6 is a condenser, 9 is a gas-liquid separator, 5 is a liquefied gasoline recoverer, and 2 and 3 is adsorption-desorption. A tower, 4 is a gas circulation blower, B1 is a closed valve except when refueling the oil supply nozzle 1, and 11 is a gasoline vapor transmission connecting the first condenser 6 and the adsorption and desorption towers 2 and 3. The engines, B11a and B11b, are adsorption valves for the adsorption and desorption towers 2 and 3 provided in the middle of the gasoline steam sending pipe 11. 120 is a pressure controller for adjusting the pressure of the adsorption and desorption towers 2 and 3, 12a and 12b are discharge pipes connecting the adsorption and desorption tower and the pressure controller 120, and B12a and B12b are provided in the middle of the discharge pipes 12a and 12b. The exhaust valves 13a and 13b of the adsorption and desorption towers 2 and 3 are purge gases used for sending a part of the clean gas discharged from the adsorption tower 2 or 3 to the atmosphere to the desorption tower 3 or 2 for use. The air supply pipes, B13a and B13b are mass flow controllers that control the amount of gas provided in the purge gas air supply pipes 13a and 13b.

14a and 14b are desorption purge gas pipes connecting the gas circulation blower 4 and the adsorption and desorption towers 2 and 3, and B14 and B14b are the adsorption and desorption towers 2 provided in the purge gas pipes 14a and 14b. , 3) a desorption valve, 201 is a refrigerator for cooling the first condenser 6 and the adsorption and desorption towers 2, 3, 202 is a temperature medium cooled by the freezer 201 to the adsorption tower (2, 3) Is a heat exchanger for transmitting the heat of the refrigerant supplied from the freezer 201 to the temperature medium, and 204 is a temperature medium tank filled with the temperature medium cooled by the heat exchanger 203.

First, the configuration of the apparatus will be described. Fig. 11 shows a layout of a gaseous hydrocarbon treatment and recovery apparatus according to an embodiment of the present invention. As shown in FIG. 11, only the refrigerator 201 is placed above the air gap 301. That is, since the refrigerator 201 does not directly contact with gasoline vapor, it is located above the air gap 301. As a result, the refrigerator 201 is provided outside the range of the flammable vapor staying place, and has a high safety arrangement in which the combustible steam does not ignite by the refrigerator 201. On the other hand, other equipment, i.e., the pump 8, the first condenser 6, the gas-liquid separator 9, the adsorption-desorption towers 2, 3, the gas circulation blower 4, the valves B11a, B11b, Since B12a, B12b, B14a, and B14b, the mass flow controllers B13a and B13b, and the pressure controller 120 (some of these are not shown) are in contact with gasoline steam, they are provided in a flammable vapor staying place. In addition, the electrical apparatus provided in the flammable vapor | staying place has an explosion-proof structure in order to ensure safety.

In addition, since the liquid circulation pump 202 and the temperature medium tank 204 are not in contact with gasoline vapor, it is natural that the liquid circulation pump 202 and the temperature medium tank 204 are normally placed above the air gap 301. However, placing the liquid circulation pump 202 above the air gap 301 is in a position higher than that of the adsorption-and-desorption towers 2 and 3 to which the liquid circulation pump 202 supplies the temperature medium. There is a concern that the air may be curled in the 202, causing a problem that the adsorption-and-desorption towers 2 and 3 cannot be cooled. Therefore, it is effective to put the liquid circulation pump 202 and the temperature medium tank 204 which have an explosion-proof structure in the place of a flammable vapor stay. In addition, it is necessary to make it possible to know the content of the temperature medium contained in the temperature medium tank 204. In other words, by providing a liquid level gauge, a water level display pipe, or the like (not shown), monitoring the content of the temperature medium can reveal a decrease in the cooling capacity of the device, thereby providing a safer recovery device.

Next, the operation will be described. When refueling is started at the gasoline stand, the pump 8 is operated to inhale the gasoline vapor leaked from the refueling nozzle 1 (about 40 vol% at room temperature), pressurized to about 0.3 MPa, and the first condensation. Is sent to the device (6). When the refrigerant is supplied from the refrigerator 201 to the heat exchanger 203 in the temperature medium tank 204, the first condensing device 6 provided in the temperature medium tank 204 is indirectly cooled through the temperature medium. . Usually, the inside of the 1st condensation apparatus 6 is maintained at 0 degreeC to 5 degreeC, the water contained in gasoline and gas is partially condensed, and gas (gasoline vapor) and liquid (gasoline) are carried out through the gas-liquid separator 9. Separated by). The liquid is stored below the first condensation apparatus 6, recovered as a liquid in the liquefied gasoline recoverer 5, and the gas is discharged from the first condensation apparatus 6. By introducing gasoline vapor from above the first condenser 6 and circulating it downward, the liquefied gasoline or water flows downward efficiently by gravity and gas flow, and the recovery of these liquefied liquids becomes easy.

By the way, the density | concentration of gasoline vapor becomes about 10 vol% on the conditions of the pressure of 0.3 MPa, cooling temperature of 5 degreeC, and gas flow rate of 601 / min which are the operating conditions of the 1st condensing apparatus 6. As shown in FIG. As can be seen from the saturation concentration line of the gasoline steam, the saturated gasoline vapor concentration is about 10 vol% at a pressure of 0.3 MPa and a temperature of 5 ° C., and in this condition, the gasoline vapor concentration is theoretically 10 vol% or less. There is nothing to be done. In addition, by lowering the temperature, the gasoline vapor concentration at the outlet of the first condensation device 6 can be reduced. However, if the set temperature is below the freezing point, the water contained in the gas freezes in the first condensing device 6, causing a problem of clogging of the pipe. Therefore, the set temperature of the first condensing device 6 is zero. It is preferable to set it as about 5 to 5 degreeC.

Subsequently, about 10 vol% of gasoline vapor which has not been processed in the first condensation apparatus 6 is sent to the adsorption-desorption towers 2 and 3 for processing. In FIG. 10, the case where the bivalent adsorption tower and 3 operate | move as a desorption tower is shown. Therefore, the valve B11a is in an open state (black fill), and the valve B11b (the inside is made white) is in a closed state. After the adsorption treatment at any time in the adsorption tower 2, it is used as a desorption tower. In this case, the valve B11a is closed and the valve B11b is used in an open state. In addition, when desorption of gasoline is complete | finished, it uses as an adsorption tower again, and this operation is used repeatedly over time. Switching of adsorption and desorption is controlled by switching of the valves B11a and B11b as described above.

The gasoline vapor is sent to the adsorption tower 2 through the exhaust pipe 11. The adsorption-and-desorption towers 2 and 3 are sealed with an adsorbent for adsorbing gasoline vapor. Silica gel was used as an adsorbent of gasoline vapor. Particularly effective are silica gels or synthetic zeolites having a pore size of 4 to 100 angstroms or mixtures thereof. As the gasoline vapor passes through the adsorbent, the gasoline component is adsorbed and removed, and becomes clean air with a gasoline concentration of 1 vol% or less, and is discharged to the atmosphere through the discharge pipe 12a. Moreover, the pressure controller 120 which controls the pressure to a prescribed value is arrange | positioned downstream of the discharge pipes 12a and 12b to air | atmosphere, and it is made to maintain the pressure in the adsorption tower 2 at a specified value. In this embodiment, since adsorption is carried out using exhaust gas of a high pressure (about 0.3 MPa) of the first condensing device 6, the adsorption capacity is significantly improved than adsorption at normal pressure.

The adsorption-desorption towers 2 and 3 are always cooled to a constant temperature by a temperature medium supplied by the liquid circulation pump 202 regardless of the role of adsorption-desorption of gasoline vapor. That is, the cooling system of the 1st condensation apparatus 6 and the adsorption-and-desorption towers 2 and 3 is always operationally controlled so that it may be maintained at a preset temperature. This is because the silica gel 21 filled in the adsorption and desorption towers 2 and 3 is cooled by heat transfer from the fin tube heat exchanger 22, so that some cooling time is indispensable, and it is possible to cope with operation in an instant. Because you can't. In addition, the provision of the refrigerator 201 having a large cooling capacity for cooling in a short time is a bad effect on the installation cost, and the inexpensive gasoline recovery device cannot be started. In addition, by lowering the temperature inside the adsorption column 2, the adsorption capacity can be increased to reduce the amount of the silica gel 21 used. However, if the internal temperature of the adsorption tower 2 is lower than the set temperature of the first condenser 6, water will condense in the adsorption tower 2, and if the temperature is below the freezing point, the first condensation will occur. It is better to set it at about the same temperature as the apparatus 6.

As described above, the cooling system of the first condensation device 6 and the adsorption-and-desorption towers 2 and 3 is maintained at a set temperature, and the first condensation device 6 and the adsorption-and-desorption towers 2 and 3 are maintained. The pressure system can perform efficient gasoline recovery by always operating control so that a pressure system may be maintained at a set pressure.

The outer structure of the adsorption-and-desorption towers 2 and 3 has a cylindrical structure, as shown in Fig. 12A. By such a structure, it becomes possible to equalize the pressure applied to the wall surface, and even if the pressure in the adsorption-and-desorption towers 2 and 3 is about 0.3 MPa, the safety is high, that is, the shape deformation is not performed. The desorption towers 2 and 3 can be realized. In addition, the internal structure of the adsorption-and-desorption towers 2 and 3 arranges a fin tube heat exchanger (a thermal medium flows through the heat transfer tube 22) in consideration of heat transfer to the silica gel 21 or the synthetic zeolite. The silica gel 21 or the synthetic zeolite is filled between the aluminum fins, the silica gel outflow prevention net 24 is provided up and down, and the silica gel 21 is prevented from flowing out into the pipe. Is doing good. In this case, in order to uniformize the adsorption of gasoline vapor to the silica gel 21, a rectifying plate 23 made of a punching metal or the like may be provided so that the gasoline vapor flows uniformly in the adsorption-desorption towers 2 and 3. . It is preferable to set the direction of the fin of the fin tube heat exchanger 22 so as to be parallel to the flow direction of the gasoline vapor so that it may not become a pressure loss when the gasoline vapor flows. That is, in the case of Fig. 12A, since gasoline vapor flows from the bottom to the top, it is laminated in the horizontal direction. In addition, in order to efficiently cool the silica gel 21 filled near the outer wall, it is necessary to prevent the gap between the fin tube heat exchanger 22 and the outer wall from occurring.

In this case, as shown in Fig. 12 (b), on the side where the vent is located, a lattice or plate metal (aluminum or copper having excellent heat transfer characteristics) which is in contact with the vent part is provided and the vent is On the absence side, it is effective to eliminate the gap between the outer wall and the fin tube heat exchanger 22 by lengthening the length of the fin itself of the fin tube heat exchanger 22. In addition, a metal rod, a pipe with a fin, or the like may be inserted so as to eliminate a gap portion between the outer wall and the fin tube heat exchanger 22. In addition, when a temperature medium flows through the heat exchanger tube of the fin tube heat exchanger 22, the piping in which a temperature medium flows before branching into a heat exchanger tube is divided, and the fin tube heat exchanger 22 is divided into several blocks, and a temperature medium is paralleled. It is better to let it flow. Thereby, the pressure loss of the piping through which a temperature medium flows can be reduced, and the capacity | capacitance of the liquid circulation pump 202 which supplies a temperature medium to the adsorption-and-desorption towers 2 and 3 can be reduced.

In addition, in this case, since gasoline vapor flows from bottom to top, it is preferable to arrange | position so that the fin tube heat exchanger 22 and the lower silica gel outflow prevention net 24 may contact. Thereby, the space between the silica gel outflow prevention net 24 and the fin tube heat exchanger 22, ie, the space filled only with the silica gel 21, can be eliminated, and the silica gel 21 is sufficiently cooled at the time of adsorption. can do. As a result, it is possible to prevent the temperature of the silica gel 21 present in the portion at which the gasoline vapor of the highest gasoline concentration enters to be raised, and provide safe adsorption and desorption towers 2 and 3. In addition, when gasoline vapor flows from the top to the bottom, it goes without saying that the upper silica gel outflow prevention net 24 and the fin tube heat exchanger 22 are in contact with each other.

When the first condensation device 6 is not provided at the front end of the adsorption and desorption towers 2 and 3, a high concentration of gasoline vapor is introduced into the adsorption and desorption towers 2 and 3 and contained in the gasoline vapor. The absorbed moisture is adsorbed to the adsorbent, and the adsorption performance of gasoline vapor is deteriorated, and an amount of the adsorbent in excess is required. In addition, when the temperature of the adsorption tower 2 is lowered below the freezing point, large troubles may occur such as water condensation on the surface of the adsorbent and clogging of the gas.

In this embodiment, since the 1st condensation apparatus 6 is provided in front of the adsorption-and-desorption towers 2 and 3, since moisture is also removed with gasoline vapor, in the adsorption-and-desorption towers 2 and 3, The bad influence of moisture can be prevented beforehand. Moreover, the quantity of gasoline processed by the adsorption-and-desorption towers 2 and 3 can be reduced significantly, and the adsorption-and-desorption towers 2 and 3 can be made small and inexpensive. In addition, in this embodiment, the high concentration (40 vol%) of gasoline recovered from the oil supply nozzle 1 can be reduced to 10 vol% with the first condensing device 6, and the adsorption and desorption towers 2 and 3 are treated. The amount of gasoline can be reduced to 25% (= 10% / 40%) of the total suction. That is, the volume of the adsorption-and-desorption towers 2 and 3 can be made about 1/4 by providing the 1st condensation apparatus 6 in front of the adsorption-and-desorption towers 2 and 3.

Next, the desorption process of gasoline vapor is demonstrated. When the gasoline adsorbed to the adsorbent is desorbed, gas is sucked from the desorption tower 3 by the gas circulation blower 4 through the purge gas delivery pipe 14a to desorb the gasoline from the adsorbent. At this time, the valve B14a is open and the valve B14b is closed. At the time of adsorption, the adsorption column is operated at a high pressure of 0.3 MPa. However, at the time of desorption, the gas circulation blower 4 reduces the pressure to atmospheric pressure or lower, so that gasoline adsorbed to the adsorbent is desorbed by this pressure difference. The desorbed gasoline vapor is returned to the first condenser 6 in FIG. 10, and the gasoline powder is condensed and recovered again, and then returned to the adsorption tower 2 again. While repeating this operation, the entire amount of gasoline is condensed and recovered in the first condensation device 6. At the time of desorption, although the desorption rate can be increased by increasing the temperature inside the desorption tower 3, the energy consumption in the refrigerator and the heater is increased by shaking the temperature. There is a problem that the switching of (2, 3) cannot be performed in a short time, and it is effective to perform desorption at the same temperature as the adsorption without raising the temperature at the time of desorption.

In addition, the outlet of the gasoline vapor from the desorption tower 3 at the time of desorption is provided in the same part of the supply port of the gasoline vapor to the adsorption tower 2 at the time of adsorption | suction and adsorption-and-desorption tower 2,3. Since the adsorption tower 2 is operated so that the gasoline vapor concentration at the outlet of the adsorption tower 2 is 1 vol% or less, gasoline vapor is adsorbed at high density near the gasoline vapor intake port of the adsorption tower 2 at the time of adsorption, and the adsorption tower 2 In the vicinity of the gasoline steam outlet, the gasoline vapor is not adsorbed very much. In order to collect the gasoline vapor discharged | emitted from the desorption tower 3 at the time of desorption efficiently by the 1st condensation apparatus 6, it is necessary to make gasoline vapor concentration as high as possible. Therefore, since the gasoline vapor can be discharged from the portion which is adsorbed at a high density, the gasoline vapor at a high concentration can be discharged, so that the gasoline vapor is adsorbed at a high density, that is, from the vicinity of the gasoline vapor suction port of the adsorption tower 2, It is better to discharge gasoline steam in the city.

Since the efficiency is not so high only by the desorption method using the pressure difference by suction of the gas circulation blower 4, it is effective to introduce purge gas from the outside. In this embodiment, a part of the clean gas discharged | emitted from the adsorption tower 2 to the atmosphere as this purge gas is sent to the desorption tower 3 by the discharge pipe 12a and the purge gas sending pipe 13a. B13a and B13b are mass flow controllers for controlling a gas flow rate passing therein. In this case, the mass flow controller B13a is in a state capable of flowing a prescribed amount of gas in an open state, and the mass flow controller B13b is closed. As a result, gas does not flow. In addition, in this embodiment, since the moisture content in gas is sufficiently low in the 1st condensation apparatus 6 of the front end, the moisture contained in purge gas hardly adversely affects the adsorbent in the desorption tower 3. .

As shown in Fig. 13A, the purge gas flow rate may be controlled at the time of desorption. However, in order to liquefy and recover the desorbed gasoline vapors to the first condensing device 6, it is well known that the gasoline vapors of the highest concentration are discharged from the desorption tower 3 as much as possible. In addition, since sending unnecessary gas into the system results in energy loss such as power of the gas circulation blower 4, it is effective to suppress the amount of purge gas to the minimum necessary. Therefore, as shown in Fig. 13 (b), it is effective to introduce a purge gas after a certain time elapses after the start of desorption. That is, since there is also a large amount of gasoline vapor immediately after the start of desorption, the purge gas is not necessary, but since the amount of gasoline desorbed with time decreases, the amount of suction gas also decreases. For this reason, it is effective to introduce a purge gas after a lapse of time from the start of desorption and to prevent a decrease in the amount of suction gas.

As the timing of introduction of the purge gas, a method of introducing the purge gas after a predetermined time has elapsed from the desorption using a timer or the like (timer method), and the internal pressure of the desorption tower 3 is a set value (hereinafter referred to as 'predetermined pressure'). A method of introducing a purge gas when reaching the gas pressure (pressure measuring method) and a method of introducing a purge gas when the gas amount of the gasoline vapor discharged from the desorption tower 3 reaches a set value (gas amount measuring method) are considered. Although the timer method is most advantageous at an initial cost, the timing at which purge gas is introduced may be deteriorated by the amount of gasoline adsorbed to the adsorption and desorption towers 2 and 3, and the effectiveness of purge gas introduction may be reduced. That is, when there is much adsorption amount, purge gas will be introduce | transduced when there is enough gasoline vapor in the desorption tower 3, and the gasoline vapor concentration discharged from the desorption tower 3 will fall. On the contrary, when the amount of adsorption is small, the time period in which the amount of gasoline vapor gas discharged from the desorption tower 3 is small increases, and gasoline vapor cannot be efficiently discharged from the desorption tower 3. The pressure measuring method and the gas amount measuring method can solve the problems of the above-described timer method and can realize efficient desorption. In the gasoline recovery device, it is indispensable to attach a pressure gauge to the piping system through which gasoline vapor flows. Therefore, the pressure measuring method is considered to be the most effective of the three methods because it can be used with their pressure gauge.

Fig. 14 shows the change of gasoline vapor concentration at the outlet of the adsorption and desorption towers 2 and 3 when the gasoline vapor is discharged from the adsorption and desorption towers 2 and 3 at 20 NL / min and the adsorption and desorption tower 2 at that time. , 3) shows the pressure change. Since adsorption conditions are 10 vol% gasoline concentration and 300 kPa, these values are initial values at the start of desorption. In addition, introduction of the purge gas started when the pressure of the adsorption-desorption towers 2 and 3 became a negative pressure, that is, when it reached 100 kPa. In this way, when the internal pressure of the adsorption-and-desorption towers 2 and 3 becomes a negative pressure, the gasoline vapor concentration becomes the maximum when the polarization point is reached (the stability region is reached), and then the gasoline concentration gradually increases. It was found to decrease. Therefore, in order to collect the desorbed gasoline vapor in the first condenser 6, the concentration of the desorbed gasoline vapor needs to be 10 vol% or more, which is the concentration at the outlet of the first condenser 6, and the gasoline concentration is It can be seen that gasoline recovery can be efficiently carried out by keeping the time period of 10 vol% or more as long as possible.

15 shows the internal pressure of the adsorption and desorption towers 2 and 3 at the time of desorption of gasoline vapor, the purge gas flow rate, the gasoline vapor concentration discharged from the adsorption and desorption towers 2 and 3, and the adsorption and desorption tower ( The relationship between the gasoline vapor flow rates discharged from 2 and 3) was investigated. Thus, in order to lower the internal pressure of the adsorption-and-desorption towers 2 and 3, it turned out that it is better to reduce the flow volume of purge gas. Moreover, it turned out that the density | concentration of the gasoline vapor discharged | emitted from the adsorption-and-desorption towers 2 and 3 can be made high by making the internal pressure of the adsorption-and-desorption towers 2 and 3 low. Therefore, the adsorption-and-desorption tower 2, 3) The gasoline vapor flow rate discharged from 3) decreases because the gasoline vapor concentration is low when the internal pressures of the adsorption and desorption towers 2 and 3 are high, and is discharged when the internal pressure of the adsorption and desorption towers 2 and 3 is low. It was found that the gas flow rate was small because it was small. In other words, it was found that an optimum region exists for operating together with the internal pressure and the amount of exhaust gas (amount of purge gas). However, in the present recovery device, the main purpose is not to discharge the gasoline vapor from the adsorption-desorption towers 2 and 3, but to how much the discharged gasoline vapor is recovered. Therefore, as mentioned above, in order to collect | recover by the 1st condensation apparatus 6, it is necessary to make the gasoline density | concentration in the discharged gas more than 10vol%, and how high can desorption concentration be from 10vol%. It is important.

FIG. 16 examines the relationship between the internal pressure of the adsorption and desorption towers 2 and 3 at the time of desorption of gasoline vapor and the amount of gasoline vapor discharged from the adsorption and desorption towers 2 and 3 per hour. The gasoline recovery amount per unit time is a difference between the concentration of gasoline vapor discharged from the adsorption and desorption towers 2 and 3 and the 10 vol% recovery limit concentration in the first condensing device 6, and the adsorption and desorption tower ( It can display by the product with the gas flow volume (purge gas flow volume) discharged from 2, 3). Thus, when the internal pressure was set to about 30 kPa, it turned out that the gasoline recovery amount per unit time is the highest. As described above, since the recovery rate in the first condenser 6 is about 75%, the recovery rate of the desorbed gasoline vapor needs to be 75% or more. This is because when the recovery efficiency of the desorbed gasoline vapor decreases, the gasoline vapor which is not recovered by the first condensation device 6 but moves from the desorption tower 3 to the adsorption tower 2 increases, and the operating efficiency as the recovery device is increased. This is because it is lowered.

Therefore, it is necessary to desorb gasoline vapor from the desorption tower 3 on the condition that 75% or more of the amount of gasoline vapor supplied to the adsorption tower 2 is collect | recovered. That is, since the gas flow rate supplied to the adsorption tower 2 is 60 NL / min and the gasoline vapor concentration is 10 vol%, the amount of gasoline vapor supplied to the adsorption tower 2 per unit time is 6 NL / min, so that desorption per unit time The amount of gasoline recovered from the tower 3 needs to be 4.5 NL / min or more. Thereby, it turned out that the internal pressure in the adsorption-and-desorption towers 2 and 3 needs to be 15-40 kPa. Moreover, it turned out that it is necessary to set the purge gas flow volume to 15-35 NL / min in order to make the pressure in the adsorption-and-desorption towers 2 and 3 into 15-40 kPa from FIG.

From the above results, the gaseous vapor can be efficiently desorbed by setting the discharge gas flow rate (purge gas flow rate) from the desorption tower 3 to 15 to 35 NL / min and the pressure in the adsorption tower 2 to 15 to 40 kPa. I knew it was.

In the gasoline stand, refueling is done in an indeterminate manner. For this reason, the pump 8 is operated only for the limited time at the time of oil supply from a viewpoint of electric power consumption reduction, and the gasoline vapor which leaks from the oil supply nozzle 1 is collect | recovered. Therefore, only in this case, clean air having a gasoline concentration of 1 vol% or less from the adsorption tower 2 is discharged to the atmosphere through the discharge pipe 12a. In the present recovery device, the air discharged from the adsorption tower 2 is also used to discharge gasoline from the desorption tower 3, so that the adsorption operation to the adsorption tower 2 and the desorption operation from the desorption tower 3 are always synchronized. It becomes. In other words, the pump 8 and the gas circulation blower 4 always perform intermittent operation in a synchronized state. By operating in this way, the desorbed gasoline vapor is diluted by the air sucked by the gas circulation blower 4, and the collection | recovery efficiency in the 1st condensation apparatus 6 does not fall. In addition, the gasoline vapor desorbed is not discharged from the oil supply nozzle 1. In addition, it is also possible to prevent intake of air sufficiently containing moisture into the desorption tower 3.

From the above, the pump 8 and the gas circulation blower 4 can perform efficient gasoline recovery by performing intermittent operation in the state always synchronized. In addition, by opening and closing the valve in accordance with the operation state of the pump 8, it becomes easy to keep the pressure in the adsorption-desorption towers 2 and 3 constant at all times.

Next, switching of the adsorption-and-desorption towers 2 and 3 will be described. In this embodiment, the case where switching of the adsorption-and-desorption towers 2 and 3 is performed using a timer is demonstrated. As described above, the gasoline vapor is adsorbed and removed by passing through the adsorption tower 2, and the gasoline concentration is discharged to the atmosphere through the discharge pipe 12a to become clean air having a gasoline concentration of 1 vol% or less. However, as the amount of gasoline vapor supplied to the adsorption tower 2 increases, the adsorption capacity of the adsorption tower 2 gradually decreases. This state continues and when the gasoline concentration at the exit of the adsorption tower 2 approaches 1 vol%, switching between the adsorption and desorption towers 2 and 3 is necessary. In the gasoline stand, since the oil supply is performed irregularly, when simply switching over time, a situation arises that the adsorption operation is performed by only one of the adsorption and desorption towers 2 and 3 depending on the oil supply timing. More than 1 vol% gasoline vapor may be discharged from the recovery device.

Therefore, it is effective to perform switching of the adsorption-and-desorption towers 2 and 3 at the integrated value of the time when the gasoline recovery device is operating. That is, when the integrated value of the time that the gasoline recovery apparatus is operating reaches a fixed time (hereinafter referred to as 'predetermined time'), the adsorption-desorption towers 2 and 3 are switched, and the integrated value is reset and again. In this case, the integration of the operating time may be performed from the beginning. Moreover, as an index which shows operation | movement of a collection | recovery apparatus, operation | movement of the gas circulation blower 4 and the pump 8 is mentioned. In this apparatus, since the gas circulation blower 4 and the pump 8 are synchronized, there is no problem even if either operation time is integrated. In addition, as the timing of the actual switching, it is better to switch the adsorption-desorption towers 2 and 3 without waiting for the pump 8 to stop immediately even if the integration time reaches a predetermined value. . Thereby, when the gasoline vapor is supplied to the adsorption-and-desorption towers 2 and 3, the adsorption-and-desorption towers 2 and 3 are not switched, and excessive pressure is not applied to the pump 8, and safe gasoline is prevented. A recovery device can be provided.

Finally, a method of controlling the gaseous hydrocarbon treatment and recovery apparatus will be described. When the recovery device is stopped, the gas circulation blower 4 and the pump 8 stop, and the valves B11a, B11b, B12a, B12b, B14a, and B14b are all in a closed state, and the mass flow controllers B13a and B13b are closed. ) Is in a closed state. When lubrication starts, the start signal from the lubricator is received, and for example, the lubrication start signal corresponding to the opening and closing operation of the lubrication nozzle 1 is received as the lubrication signal, and the valves B11a, B12a, and B14a are opened. After that, the gas circulation blower 4 and the pump 8 operate. When the pressure in the desorption tower 3 falls to a predetermined concentration by the operation of the gas circulation blower 4, the mass flow controller B13a starts to open, and the mass flow flows so that a predetermined flow rate flows through the desorption tower 3. The opening degree of the controller B13a is controlled. When lubrication is completed, the stop signal from the lubricator is received, the gas circulation blower 4 and the pump 8 stop, the mass flow controller B13a is closed, and the valves B11a, B12a, and B14a are closed. It is closed.

In this way, when oil supply is repeated and when the integrated value of the time of oil supply reaches predetermined time, switching of the adsorption-and-desorption towers 2 and 3 is performed. However, even when oil supply integration time reaches predetermined time during oil supply, it operates as it is until it receives the stop signal from an oil supply machine. When the stop signal is received, as described above, the gas circulation blower 4 and the pump 8 stop, the mass flow controller B13a is closed, and the valves B11a, B12a, and B14a are closed. . Next, upon receiving the start signal from the oil feeder, the integration time timer is reset, the valves B11b, B12b, and B14b are opened, and the gas circulation blower 4 and pump 8 then operate, and the adsorption tower (3) becomes adsorption operation, and the desorption tower 2 becomes desorption operation. When the pressure in the desorption tower 2 decreases to a predetermined concentration by the operation of the gas circulation blower 4, the mass flow controller B13b starts to open and the mass flow flows so that a predetermined flow rate flows through the desorption tower 2. The opening degree of the controller B13b is controlled. When lubrication is completed, the stop signal from the lubricator is received, the gas circulation blower 4 and the pump 8 stop, the mass flow controller B13b is closed, and the valves B11b, B12b, and B14b are closed. It is closed. Thereafter, this operation is repeated until the oil supply integration time reaches a predetermined time.

In the above-described embodiment, the case where the oil supply start and stop signals are received in accordance with the opening and closing operation of the oil supply nozzle 1 as the oil supply signal has been described, but the oil supply start is performed in accordance with the operation of separating the oil supply nozzle 1 from the oil supply machine. And a stop signal. In this case, however, even when the oil supply nozzle 1 is separated from the oil supply machine and the oil supply nozzle 1 is not refueled, the gaseous hydrocarbon treatment and recovery device is operated, and the recovery device is operated without inhaling gasoline vapor. There is a problem in terms of energy saving. Therefore, if such a state continues for a certain time, it is necessary to mount a control mechanism for stopping the recovery device.

As described above, the gaseous hydrocarbon treatment and recovery apparatus according to the present embodiment combines the first condensation apparatus 6 and the adsorption and desorption towers 2 and 3, so that at most 1 vol% of gasoline vapor can be obtained. It is a device for treating and recovering gaseous hydrocarbons which is only discharged and has a very low environmental load. In addition, since only 1 vol% of gasoline vapors are discharged at the maximum, up to 39 vol% of 40 vol% of gasoline vapors can be recovered, and the recovery efficiency is 97.5%. In addition, since the adsorption operation is performed after the condensation operation, the adsorption and desorption towers 2 and 3 can be miniaturized and the whole apparatus can be made compact. In addition, since the recovery of the gasoline vapor is performed in conjunction with the oil supply unit, unnecessary operation can be reduced, and the operating capital can be reduced.

[Eighth Embodiment]

It is a figure which shows the apparatus structure of the processing and collection | recovery apparatus of the gaseous hydrocarbon which concerns on 8th Embodiment of this invention.

The difference from the seventh embodiment described above is that the auxiliary temperature medium tank 205 is provided above the air gap 301, and the liquid circulation pump 202 is placed above the air gap 301. According to this embodiment, it is not necessary to make the liquid circulation pump 202 used in FIG. 11 into explosion proof structure. However, when gas (air or the like) invades the liquid circulation pump 202, there is a problem that the liquid cannot be sent. In order to prevent such a problem from occurring, the auxiliary temperature medium tank 205 is provided above the air gap 301, and the system can be stably operated by preventing gas from entering the liquid circulation pump 202.

As described above, in the present embodiment, since the liquid circulation pump 202 does not need to have an explosion-proof structure, the cost of the liquid circulation pump 202 can be reduced, and the gaseous hydrocarbon treatment and recovery apparatus can be low cost. Can be mad.

[Ninth Embodiment]

Fig. 18 is a structural diagram showing a gas circulation blower and a pump in the gaseous hydrocarbon processing and recovery apparatus according to the ninth embodiment of the present invention.

In the gaseous hydrocarbon processing and recovery apparatus of the present embodiment, the gas circulation blower 4 and the pump 8 are operated in synchronization, so that the motor 10 is shared and the gas circulation blower 4 is driven by pulley driving. The pump 8 is operated. Thereby, the initial cost of the motor 10 can be reduced and a cheap gaseous hydrocarbon treatment and recovery apparatus can be supplied.

[Tenth Embodiment]

19 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a tenth embodiment of the present invention.

In the seventh embodiment, the gasoline component is adsorbed and removed by passing through the adsorption and desorption towers 2 and 3, and the gas is discharged to the atmosphere through the discharge pipe 12a as clean air having a gasoline concentration of 1 vol% or less. In this embodiment, the ejector 211 is provided in the discharge pipe 12a so as to further reduce the gasoline concentration of the discharged gasoline vapor. This can provide a safer treatment and recovery of gaseous hydrocarbons.

[Eleventh Embodiment]

20 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to an eleventh embodiment of the present invention.

In the seventh embodiment, the integrated value of the operating time of the gas circulation blower 4 or the pump 8 is calculated, and when the value reaches the set value and the pump 8 stops next, the adsorption-and-desorption tower Although the case where switching of (2, 3) is performed was shown, in this embodiment, the gasoline concentration sensor 212 is provided in the discharge pipe 12a, and the output value from the gasoline concentration sensor 212 reaches the set value, Next, the adsorption-and-desorption towers 2 and 3 are switched when the pump 8 is stopped. This can provide a safer treatment and recovery of gaseous hydrocarbons. As the gasoline concentration sensor 212, a gasoline component is adsorbed to a semiconductor element, and the absorption amount of infrared rays having a wavelength of about 3.3 mu m is measured by using a semiconductor method for measuring the resistance of the semiconductor element or a non-dispersive infrared absorption method. Infrared absorption type is mentioned.

As such, by providing the gasoline concentration sensor 212 in the discharge pipe 12a, clean air having a gasoline concentration of 1 vol% or less can always be discharged, and a safe gaseous hydrocarbon treatment and recovery apparatus can be provided. In addition, by using the switching of the adsorption-desorption towers 2 and 3 by the gasoline concentration sensor 212 and the switching of the adsorption-desorption towers 2 and 3 by the timer described in the first embodiment, a safer gas is used. It can be set as the processing and recovery apparatus of a state hydrocarbon. That is, when the switching to the gasoline concentration sensor 212 is mainly controlled, the operation integration time of the gas circulation blower 4 is monitored, and the gasoline concentration sensor is not switched even when the predetermined set value is reached. It may be determined that 212 is abnormal and the switching is performed. Alternatively, when the switching to the operation integration time of the pump 8 is mainly controlled, the gasoline concentration in the exhaust gas is monitored by the gasoline concentration sensor 212, and the switching does not occur even when the predetermined gasoline concentration is reached. May determine that the adsorbent is abnormal in performance and perform the conversion.

[Twelfth Embodiment]

Fig. 21 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a twelfth embodiment of the present invention.

In the seventh embodiment, the temperature medium accumulated in the temperature medium tank 204 including the heat exchanger 203 is cooled by flowing a refrigerant from the freezer 201 to the heat exchanger 203, and the cooled temperature medium. Is supplied to the adsorption-and-desorption towers 2 and 3 by the liquid circulation pump 202, but the present embodiment uses a thermistor sensor such as a thermocouple on the temperature medium discharge side of the liquid circulation pump 202. The thermometer 213 formed is provided, and the thermometer 213 is used to control the operation of the refrigerator 203. Thereby, the temperature of the adsorption-and-desorption towers 2 and 3 can be controlled more accurately, and the amount of gasoline vapor discharged from the adsorption-and-desorption towers 2 and 3 can be stabilized. Therefore, a safer gas treatment and recovery apparatus for gaseous hydrocarbons can be provided.

In addition, when the thermometer 213 is provided on the temperature medium discharge side of the liquid circulation pump 202, the thermometer 213 needs to have an explosion-proof structure. Therefore, the pipe through which the temperature medium flows may be extended to an upper portion than the air gap 301, and the thermometer 213 may be provided at a portion above the air gap 301. Thereby, the thermometer 213 does not need to have an explosion-proof structure, and there exists an effect which can reduce the cost of the whole apparatus.

In addition, although the above-mentioned thermometer 213 was described about the case of thermistor sensor, such as a thermocouple, you may make it use the bellows sensor for the thermometer 213 (not shown). Normally, a bellows sensor is a bellows (a lantern-shaped container) in which a liquid or a gas is sealed inside a thermostat for sensing a temperature, and increases or decreases by volume expansion caused by the temperature detected by the thermostat. It consists of a micro switch which is contacted by an extension of the bellows. In the case of the bellows sensor, only the thermosensitive tube part can be installed in the flammable vapor staying place lower than the air gap 301, and the bellows and the micro switch can be installed in the non-explosion-proof area, so that the entire thermometer 213 is explosion-proof. There is no need to do it, and there is an effect that the cost of the whole installation can be reduced.

Although not shown, the temperature medium supplied to the adsorption and desorption towers 2 and 3 and the temperature medium discharged from the adsorption and desorption towers 2 and 3 are monitored by a thermometer 213, and the adsorption and desorption tower ( You may perform control which detects the abnormality in 2, 3). As a result, a safer recovery device can be provided.

[Thirteenth Embodiment]

Fig. 22 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a thirteenth embodiment of the present invention.

In the seventh embodiment, a case in which oil supply start and stop signals are received in accordance with the opening and closing operation of the oil supply nozzle 1 as the oil supply signal is shown, but the present embodiment uses the pressure regulating valve 214 and the filter 215. It is provided between the oil supply nozzle 1 and the pump 8, and when the gas circulation blower 4 and the pump 8 are operated simultaneously, the gas of the predetermined flow volume flows into the pump 8, and oil supply In accordance with the separating operation from the oil feeder of the nozzle 1, the oil supply start and stop signals are received.

Thus, the gas circulation blower 4 and the pump 8 can be operated at the same time even when gasoline vapor is not sucked from the oil supply nozzle 1, and the oil supply nozzle 1 is opened and closed intermittently to supply oil. Even in this case, the response can be simplified. In addition, even when the oil supply nozzle 1 is separated from the oil supply machine and the oil supply nozzle 1 is not refueled, the gaseous hydrocarbon processing and recovery device is operated, and the recovery device is operated without inhaling gasoline vapor, thereby saving energy. In view of the problem. Therefore, when such a state continues for a certain time, it is necessary to mount a control mechanism so that a collection | recovery apparatus may stop.

As described above, the pressure regulating valve 214 and the filter 215 are provided between the oil supply nozzle 1 and the pump 8, and oil supply starts and stops according to the separating operation from the oil supply unit of the oil supply nozzle 1. By receiving the signal, the operation of the gaseous hydrocarbon processing and recovery apparatus can be simplified, and the control mechanism can be reduced in cost.

[14th Embodiment]

23 and 24 are overall configuration diagrams showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fourteenth embodiment of the present invention.

In 7th Embodiment, although the case where the amount of purge gas supplied to the desorption tower 3 by the mass flow controllers B13a and B13b at the time of desorption of gasoline vapor was shown, this embodiment was shown in FIG. As described above, the rectified flow rate valves B101a and B101b and the valves B102a and B102b which flow only in a constant gas flow rate are provided so that the set flow rate flows. In addition, as shown in FIG. 24, the constant pressure valves B103a and B103b and the valves B102a and B102b, in which the pressure in the desorption tower 3 becomes a set pressure, are provided, and the pressure in the desorption tower 3 at the time of desorption. May be made constant.

As mentioned above, expensive mass flow controllers B13a and B13b are not used by combining the valves B102a and B102b with the rectifier valves B101a and B101b or the constant pressure valves B103a and B103b. And a cheap gaseous hydrocarbon treatment and recovery apparatus can be provided.

[Fifteenth Embodiment]

25 and 26 are overall configuration diagrams showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a fifteenth embodiment of the present invention.

In the fourteenth embodiment, the purge which is supplied to the desorption tower 3 using a combination of the valves B102a and B102b and the rectifier valves B101a and B101b or the constant pressure valves B103a and B103b at the time of desorption of gasoline vapor. Although the case where gas amount was controlled was shown, in this embodiment, as shown in FIG. 25, a desorption tower is carried out by two valves B102a and B102b and one rectification valve B101 by changing gasoline steam piping. The flow rate is set in (3). In addition, as shown in FIG. 26, the pressure in the desorption tower 3 is fixed at the time of desorption by using two valves B102a and B102b and one static pressure valve B103 by changing gasoline steam piping. It may be done.

As described above, by changing the gasoline steam pipe and using the valves B102a and B102b in combination with the rectifier valve B101 or the constant pressure valve B103, the rectifier valve B101 or the constant pressure valve B103 is used. The use amount of can be reduced, the cost of the system can be reduced, and an inexpensive gaseous hydrocarbon treatment and recovery apparatus can be provided.

[16th Embodiment]

Fig. 27 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a sixteenth embodiment of the present invention.

In the seventh embodiment, a case where temperature control of the adsorption and desorption towers 2 and 3 is performed by supplying a temperature controlled temperature medium to the adsorption and desorption towers 2 and 3 by the liquid circulation pump 202 is shown. In this embodiment, the temperature sensor 216 for measuring the temperature of the adsorbent is provided in the adsorption-desorption towers 2 and 3 so as to control the operation of the liquid circulation pump 202 so that the adsorbent is at a set temperature. . Thereby, the energy consumed by the liquid circulation pump 202 can be reduced, and an apparatus for treating and recovering gaseous hydrocarbons with a small operating capital can be provided. In addition, as an attachment position of the temperature sensor 216, it is better to provide it on the supply side of the gasoline vapor of the adsorption-and-desorption towers 2 and 3. In this position, since the adsorption and desorption of gasoline vapor to the adsorbent is the most severe, the temperature change of the adsorbent is increased, and the temperature control according to the temperature change can be performed quickly.

Moreover, by providing the temperature sensor 216 and monitoring the temperature change of the adsorption-and-desorption towers 2 and 3, it is possible to confirm whether the adsorption-and-desorption operation is being performed stably, and the safety of the gaseous hydrocarbon treatment and recovery apparatus. Can increase.

As mentioned above, by providing the temperature sensor 216 which measures the temperature of the adsorption agent in the adsorption-and-desorption towers 2 and 3, operation fund can be reduced and safer operation can be realized.

[17th Embodiment]

FIG. 28 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a seventeenth embodiment of the present invention. FIG.

In the seventh embodiment, when the gas circulation blower 4 and the pump 8 are operated at the same time, they are pressurized by the adsorption tower 2 to adsorb gasoline vapor, and the gas is decompressed by the desorption tower 3 to desorb the gasoline vapor. In this embodiment, the pressure sensor 217 is provided on the discharge side of the pump 8 and the suction side of the gas circulation blower 4, respectively. Thereby, the pressure of the discharge side of the pump 8 and the pressure of the suction side of the gas circulation blower 4 can be monitored, and it is possible to confirm whether the gas circulation blower 4 and the pump 8 are operating normally. .

Thus, by providing the pressure sensor 217 on the discharge side of the pump 8 and the suction side of the gas circulation blower 4, the pressure of the gasoline vapor distribution line can always be monitored and the safe gaseous hydrocarbon It is possible to provide a treatment and recovery apparatus.

In the above description, the case where the pressure sensor 217 is provided on the discharge side of the pump 8 and the suction side of the gas circulation blower 4 is shown. However, as shown in FIG. 29, the pressure sensor 217 is shown. ) May be attached to each of the adsorption-and-desorption towers 2 and 3. Thereby, it can monitor that the pressure in the adsorption-and-desorption towers 2 and 3 became pressurization or pressure reduction, and it can confirm whether the gas circulation blower 4 and the pump 8 operate normally. In this case, it is also possible to check whether the valves B11a, B11b, B12a, B12b, B14a, and B14b and the mass flow controllers B13a and B13b are operating normally.

As described above, by providing the pressure sensors 217 in each of the adsorption and desorption towers 2 and 3, the pressure in the adsorption and desorption towers 2 and 3 can always be monitored, and the safer treatment of gaseous hydrocarbons and A recovery device can be provided.

[Eighteenth Embodiment]

30 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to an eighteenth embodiment of the present invention.

In 7th Embodiment, although the case where the gasoline vapor suctioned from the oil supply nozzle 1 via the pump 8 was supplied directly to the 1st condensation apparatus 6 was shown, this embodiment is the pump 8 The gas line is branched at the discharge side of the gas supply line, and a gas line 218 which does not pass through the first condensation device 6 is provided, and valves B104 and B105 are provided in each line. As a result, even when gasoline vapor having a temperature lower than the set temperature of the first condenser 6 is supplied from the pump 8, the water contained in the gasoline vapor in the first condenser 6 freezes. As a result, clogging of the pipe can be prevented in advance, and the gasoline vapor can be recovered stably. In addition, as a measurement part of temperature, a gasoline vapor distribution line and external air are considered.

In this case, the temperature of the gasoline vapor passing through the pump 8 may be monitored, and the valves B104 and B105 may be operated at the temperature, and the temperature of the outside air is monitored, and the valves B104 and B105) may be operated. However, since the outside air is also blown in when the gasoline vapor is sucked out from the oil supply nozzle 1, the temperature of the gasoline vapor-containing air follows the outside temperature, so that a sufficient effect can be obtained even if controlled at the outside temperature. In addition, since the outdoor air temperature does not change rapidly, the valves B104 and B105 can be operated stably, and the system can be easily controlled.

In this way, the gas line is branched at the discharge side of the pump 8 to provide the gas line 218 which does not pass through the first condensing device 6, and the valves B104 and B105 are provided at the respective lines. As a result, clogging of the pipe in the first condensation device 6 can be prevented in advance, and a safe gaseous hydrocarbon treatment and recovery device can be provided.

[19th Embodiment]

It is explanatory drawing which shows the structure of the adsorption-and-desorption tower which concerns on 19th Embodiment of this invention.

In the seventh embodiment, the outer structure of the adsorption-desorption towers 2 and 3 is a cylindrical structure, the fin tube heat exchanger 22 is disposed therein, and the silica gel 21 or the synthetic zeolite alone between the aluminum fins. Or although it showed about the case where these mixtures are filled, in this embodiment, the some cylindrical tube 31 is arrange | positioned in parallel, the silica gel 21 or the synthetic zeolite alone or these in the cylindrical tube 31 is provided. The mixture is filled and a temperature medium flows around the cylindrical tube 31. Thereby, the silica gel 21 or the synthetic zeolite alone or a mixture thereof can be uniformly cooled in the cylindrical tube 31, and gasoline vapor can be stably adsorbed and removed.

In this case, as shown in FIG. 32, the end surface of the adsorption-and-desorption towers 2 and 3 is divided into a plurality of hexagons 32, and a cylindrical tube 31 is provided so as to be inscribed in the hexagons 32, and the adsorption tower By arranging the cylindrical tube 31 regularly in (2, 3), the adsorption-and-desorption towers 2, 3 can be filled with the silica gel 21 or the synthetic zeolite alone or a mixture thereof. It is possible to uniformly cool the silica gel 21 or the synthetic zeolite alone or a mixture thereof in all the cylinder tubes 31. In addition, although not shown in the figure, a baffle plate may be provided outside the cylindrical tube 31 to prevent the temperature medium supplied from the lower portion to the adsorption-and-desorption towers 2 and 3 from short-passing.

As described above, the plurality of cylindrical tubes 31 are inserted into the adsorption-and-desorption towers 2 and 3, and the adsorbent is cooled more uniformly by having a structure in which a temperature medium flows through the outer wall of the cylindrical tubes 31. It is possible to provide a gaseous hydrocarbon treatment and recovery apparatus with stable gasoline removal performance.

[20th Embodiment]

Fig. 33 is an external view of an apparatus for treating and recovering gaseous hydrocarbons according to a twentieth embodiment of the present invention.

In this way, the positions of the pipes and the valves may be changed so that the shelf 33 can be provided. This eliminates the need to install the service equipment shelf installed in the gasoline stand, and allows the present recovery device to be placed in the space in which the service equipment shelf is placed, thereby saving space in the gasoline stand.

As described above, by changing the pipe and valve positions so that the shelf 33 can be installed, the service part shelf can be eliminated, and the gaseous hydrocarbon treatment and recovery device can be installed in the space, thereby emptying the gasoline stand. Space can be secured.

[21st Embodiment]

Fig. 34 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a twenty-first embodiment of the present invention.

In the first embodiment, two towers are provided with the adsorption and desorption towers 2 and 3, and the adsorption and desorption towers 2 and 3 of the first tower are operated by different functions, such as the adsorption tower 2 and the desorption tower 3. Although the case where the operation | movement was changed alternately and the adsorption-and-desorption operation was shown was shown, in this embodiment, the adsorption-and-desorption tower 2 is provided only one tower. 219 is a dry air generator for supplying dry air to the adsorption-and-desorption tower 2, 220 is a gas storage tank which temporarily stores desorbed gasoline vapor, and B106, B107, and B108 are valves.

Next, the adsorption operation of gasoline vapor will be described. When fueling is started at the gasoline stand, the valves B1, B11, B12, B106, and B108 are opened, the pump 8 and the gas circulation blower 4 are operated, and the gasoline vapor leaked from the oil supply nozzle 1 (About 40 vol% at room temperature) is sucked in, for example, pressurized to about 0.3 MPa, and is sent to the first condensing device 6. At this time, when the refrigerant is supplied from the refrigerator 201 to the heat exchanger 203 in the temperature medium tank 204, the first condensation device 6 provided in the temperature medium tank 204 is indirectly through the temperature medium. It is maintained at about 0 ° C to 5 ° C, and water contained in gasoline and gas is partially condensed and separated into gas (gasoline vapor) and liquid (gasoline) through the gas-liquid separator (9). The liquid is stored below the first condensation apparatus 6, recovered as a liquid in the liquefied gasoline recoverer 5, and the gas is discharged from the first condensation apparatus 6. At this time, the gas circulation blower 4 is also operated, and gasoline vapor is sucked from the gas storage tank 220 through the valve B108, and the pressure in the gas storage tank 220 decreases. When the pressure of the gas reservoir 220 reaches a predetermined value, the valve B108 is closed and the gas circulation blower 4 stops. Meanwhile, about 10 vol% of gasoline vapor not processed by the first condenser 6 is sent to the adsorption-and-desorption tower 2 for treatment, and the gasoline vapor in the adsorption-and-desorption tower becomes clean air to operate the pressure controller 120. Through the atmosphere.

Next, the desorption operation will be described. After the adsorption treatment at any time in the adsorption and desorption tower 2, the pump 8 is stopped, the valves B1, B11, B12, B106, and B108 are closed, and desorption starts. Thereafter, the valves B14 and B107 are opened, the gas circulation blower 4 is operated, and the gasoline vapor is sucked and desorbed from the adsorption-and-desorption tower 2. Gasoline vapor discharged from the adsorption-and-desorption tower 2 is supplied to the gas storage tank 220 by the gas circulation blower 4. When the pressure in the adsorption-and-desorption tower 2 reaches a predetermined value, the dry air generator 219 is operated, the dry air is supplied to the adsorption-and-desorption tower at a constant flow rate, and the desorption of gasoline vapor is promoted by the gas purge of the dry air. do. Thereafter, when the pressure in the gas reservoir 220 reaches a predetermined value, the valves B14 and B108 are closed, and the gas circulation blower 4 and the dry air generator 219 stop. In this way, when desorption of gasoline is complete | finished, it uses as an adsorption tower again, and this operation is used repeatedly in time. By operating in this way, the gasoline in gasoline vapor can be liquefied and recovered, and clean air with a gasoline concentration of 1 vol% or less can always be discharged. However, since it is necessary to repeat the adsorption and desorption operation in time, it is difficult to apply the case of treating gasoline steam continuously.

In the above description, the case where the dry air generator 219 is provided has been described. However, the gasoline in the gasoline vapor is liquefied even if the dry air generator 219 is removed by increasing the capability of the gas circulation blower 4. In addition to being able to recover, clean air with a gasoline concentration of 1 vol% or less can always be discharged.

As mentioned above, in this embodiment, the adsorption-and-desorption tower 2 is made into 1 tower, and by providing the gas storage tank 220, the control which switches the adsorption-and-desorption tower 2 is unnecessary, and the adsorption-and-desorption tower is The cost of (2) can be reduced, and the control and recovery apparatus of a cheap gaseous hydrocarbon of simple control can be provided.

[22nd Embodiment]

35 is an overall configuration diagram showing a flow of a gaseous hydrocarbon treatment and recovery apparatus according to a twenty-second embodiment of the present invention.

In the seventh embodiment, a case where clean air having a gasoline concentration of 1 vol% or less is discharged to the atmosphere through the pressure controller 120 is shown. In this embodiment, the frame arrester is downstream of the pressure controller 120. 221 is provided so that even if the fire comes from the outside, the fire does not reach inside. In this way, it is possible to prevent the external fire from invading the inside, and to provide a safer gaseous hydrocarbon treatment and recovery apparatus. Although not shown, the same effect can be obtained by providing the frame arrester 221 in the flow passage through which the liquefied gasoline discharged from the liquefied gasoline recoverer 5 flows.

According to the present invention, the exhaust gas can be extremely clean (gasoline concentration of 1 vol% or less) by providing a condensation device for removing water and gasoline vapor and a gas adsorption and desorption device, and furthermore, a compact and inexpensive gasoline vapor. A recovery device can be realized. In particular, even when the gasoline vapor contains water, there is no fear that the adsorbent is poisoned with water, and no freezing occurs in the piping of the condenser or the adsorption-and-desorption device, so that stable operation can be realized.

In addition, by controlling the temperature of the heat medium to a constant temperature and controlling the temperature of the condensation device and the adsorption and desorption device, the control circuit can be simplified and the cost can be reduced as compared with the case of individually controlling each device. Can be. In addition, since the temperature of the adsorption tower is made constant irrespective of adsorption and desorption, the energy required to cool the adsorption tower can be reduced, and an energy-saving gasoline vapor recovery device can be realized. In addition, since the adsorption tower is cooled, a large amount of gasoline vapor can be adsorbed with a very small amount of adsorbent, and the amount of the adsorbent used can also be reduced.

In addition, it is possible to suppress an abnormal temperature rise in the adsorption column due to the heat of adsorption, thereby making it possible to uniformize the temperature in the adsorption apparatus and to ensure the safety of the adsorption apparatus.

Claims (9)

An apparatus for treating and recovering gaseous hydrocarbons for treating gasoline vapor leaking during gasoline refueling, A first condensation device 6 for removing water and gasoline vapor and a gasoline vapor adsorption / desorption device 2 provided on the gas downstream side of the first condensation device are provided. And recovery device. The method of claim 1, A plurality of said condensing apparatuses are provided, and the gas which is not processed by the said 1st condensing apparatus 6 is processed by the 2nd condensing apparatus 7 set to a temperature lower than a 1st condensing apparatus. Apparatus for the treatment and recovery of state hydrocarbons. The method according to claim 1 or 2, The adsorption-and-desorption device is provided with two towers, one tower 2 is operated as the adsorption tower and the other tower 3 as the desorption tower, and when a predetermined time elapses, the function is reversed to treat gasoline vapor. Apparatus for treating and recovering gaseous hydrocarbons, characterized in that A first condensing device (6) for removing water and gasoline vapor contained in the gasoline vapor, and a gas downstream side of the first condensing device; A gasoline vapor adsorption and desorption device 2 is provided, the gasoline vapor is supplied to the first condensation device and the adsorption tower of the adsorption and desorption device at the time of refueling, and the desorption and desorption of the desorption device is synchronized with the operation. A gaseous hydrocarbon processing and recovery apparatus characterized by discharging gasoline vapor from the tower and returning the desorption gas to the condenser. The method according to claim 1 or 4, A fin tube heat exchanger is provided inside the adsorption-and-desorption device (2), and a single or mixture of silica gel or synthetic zeolite having a pore diameter of 4 to 100 angstroms, which is an adsorbent, is filled between the fins of the fin tube heat exchanger. An apparatus for treating and recovering gaseous hydrocarbons. The method according to claim 1 or 4, Apparatus for treating and recovering gaseous hydrocarbons, characterized by controlling the temperature of the first condensation apparatus 6 and the adsorption and desorption apparatus 2 to an isothermal temperature using a temperature medium temperature controlled by a refrigeration or cooling device. . delete delete delete

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