TWI327164B - - Google Patents

Description

1327164 IX. Description of the Invention: [Technical Field] The present invention relates to a treatment and recovery apparatus for gas-like carbon and nitrogen contained in an atmosphere-releasing gas, and a method thereof, and more particularly to an oil supply facility at a gas station or the like And an apparatus and method for treating volatile flammable gasoline vapor such as gasoline. [Prior Art] In the conventional method for removing gaseous hydrocarbons using an adsorption desorbent, the gas generated by the exhaust gas generation source (containing about 40 vol% of gasoline vapor) is supplied from the exhaust gas supply pipe by the air blower or its own pressure. Exhaust gas) is supplied to the adsorption tower, and the treated exhaust gas at the end of the adsorption step is passed through the discharge pipe from the top of the adsorption tower (being the desorption step after the desorption step) as a gasoline vapor containing less than 1 vol%. The air (clean gas) is discharged to the atmosphere. In this case, the adsorption tower is operated while switching the adsorption step and the desorption step described later alternately, but the switching time is set to about 5 minutes (Switching Time) » On the other hand, after the adsorption step is completed In the adsorption tower, the flushing gas is supplied to the gas through the purge gas supply pipe, and is sucked by the vacuum pump to be desorbed. As the flushing gas, a part of the clean gas discharged from the top of the adsorption tower during the adsorption operation was used, and the vacuum pump was operated at about 25 Torr. The degassing rinsing exhaust gas containing gasoline vapor is supplied to the gasoline recovery device via the air supply pipe and is contacted with the liquid gasoline via the distribution pipe, and is used as a liquid (gasoline absorbing liquid) to recover the gasoline vapor β in the rinsing exhaust gas. In the exhaust gas from the gasoline recycler, because the residual trace of gasoline is steamed 2118-8326-PF 5 1327164, it is returned to the exhaust pipe via the return pipe, and the exhaust hole from the gas generating source is subjected to adsorption treatment, and The adsorbent layer in the adsorption tower is cooled, and the cooling water is circulated in the inner tube. With such a configuration, the gasoline vapor can be recovered as a full amount of liquid gasoline, and the concentration of the gasoline vapor discharged from the adsorption tower can be reduced to a level that does not cause atmospheric pollution (for example, refer to the patent document 〇. [Patent Document 1] [Problem to be Solved by the Invention] In the method of recovering gasoline vapor by vacuum fruit in Patent Document 1, the kinetic energy of the pump becomes extremely large, and It is impractical. In addition, because of the large amount of enthalpy; the 隹彡-human pupil is fully absorbed, it is necessary to make the adsorption tower bigger, or shorten the adsorption and thawing and switching time (Switching)

Time) ‘but using the sound of a large adsorption technique

It is. The problem of the residual set area or the cost of the adsorbent. When the switching time is changed again, there is a problem that the adsorbed gasoline vapor is sufficiently solved and the life of the valve or the like is shortened. Further, in the case where the adsorption tower is made large, the pressure loss of the adsorption tower becomes large, and the problem of high-efficiency treatment is caused. And the use of a large amount of adsorbent, the flow of the rational gas is slow, and there is no way, although the gasoline vapor must contain the right side of the name to hit 3 of the water in the air, but in the past way 'because it is hard with gasoline vapor · This water; 7 is also adsorbed at the same time, so there is a problem that the adsorption performance of the adsorbent is lowered. 2118-8326-PF 6 1327164 Further, in the case of recovery of gasoline vapor which is leaked from the underground storage tank of the oil supply station, a large amount of generated gasoline vapor needs to be treated in the time zone for supplying oil to the underground storage tank. Therefore, it is necessary to design the device performance in conjunction with the peak amount, = to make the device performance beyond what is required. The present invention has been made to solve the above problems, and an object of the present invention is to provide a gas-like hydrocarbon treatment and recovery apparatus and a method thereof, which prevent the adsorbent from being poisoned by the influence of moisture contained in gasoline vapor, and are smaller. Cheap. _ [Means for Solving the Problem] The gas-like hydrocarbon treatment and recovery device of the present invention is a treatment and recovery device for treating gaseous hydrocarbons of gasoline vapor leaked during supply of gasoline, characterized in that it includes: removing moisture and a first condensing device for gasoline vapor, a second condensing device for removing gasoline vapor, a gas downstream side disposed at a later stage of the first condensing device; and an adsorption and desorption device for gasoline vapor, a gas disposed at a later stage of the second condensing device Downstream side. Further, the method for treating and recovering gaseous hydrocarbons according to the present invention is a treatment and recovery apparatus for treating gaseous hydrocarbons of gasoline vapor leaking during the supply of gasoline, including: removal of moisture and gasoline vapor - a coagulation device; a first coagulation device that removes > fly oil vapor is disposed on the downstream side of the gas after the first coagulation device; and an adsorption desorption device for the gasoline vapor, which is disposed in the subsequent stage of the second coagulation device The downstream side of the gas is characterized in that: the adsorption desorption device has at least one adsorption tower and a desorption tower, which are processed in a sequence higher than 〇 ° C, higher than a space of 3 (the space of the TC, and the space filled with the adsorbent). [Invention Effect] 2118-8326-PF 7 1327164 The present invention is provided by: a first coagulation device for removing moisture and gasoline vapor, a second coagulation device for removing gasoline vapor, and adsorption and removal of gasoline vapor. The desorption device can make the exhaust gas extremely clean (gasoline concentration is lower than ivol%)' and can realize a small and inexpensive recovery device. Especially, even in π oil In the case where the gas contains moisture, it is also necessary to prevent the adsorbent from being subjected to water knife poisoning α and not to freeze in the piping of the first coagulation device or the adsorption desorption column, so that stable operation can be achieved. Two temperature zones separate the function of water and gasoline back and charge, which can reduce the moisture knot; the energy waste caused by the east can realize the energy-saving gasoline vapor recovery device. In addition, by making the first The coagulation, the device and the adsorption desorption column are indirectly cooled, and the second coagulation device performs direct cooling, which not only opens and closes the refrigerating machine, but also controls the operation of the coagulation device by controlling the flow of the refrigerant, thereby realizing energy-saving gasoline. a vapor recovery device. Further, since the second condensation device is provided to efficiently recover the gasoline vapor, the gasoline vapor is supplied to the first adsorption desorption column, so that the oil vapor can be adsorbed with a very small amount of the auxiliary agent. Reducing the amount of adsorbent used. Further, after the gasoline adsorption operation is completed, the first adsorption desorption tower is stored by taking time to store it. In the recovery operation of the gasoline, the performance of the desorption-related machine attached to the first adsorption-desorption column can be reduced, and an inexpensive gasoline-gas recovery device can be realized. [Embodiment] FIG. 1 is a view showing the present invention. 2118-8326-PF 8 丄 164 of the first embodiment of the present invention, the overall structure of the process of the treatment and recovery device. In the first figure, the gasoline storage tank is supplied to the gasoline storage tank, and the gasoline system is supplied. In the case of the oil f, the air is contained in the air_^; and the second two-way switching valve 3a is used to discharge the gasoline vapor to the atmosphere. The pressure regulating valve '5 series refrigerator, 6 series and the freezing machine. Temporary brain 7 / mill 5 connected to cool the temperature of the household medium; 7 heat exchanger, 7 series contain the temperature of the heat exchanger 6 cooling, medium temperature medium tank, 8 series sent by the temperature medium tank 7 has been cooled The temperature-media liquid circulation pump, the 9th system uses the temperature medium-cooled first-condensation device sent by the liquid circulation pump 8, the 1G system refrigeration, and the east machine 5 cools the second condensation device '11 series, using the liquid circulation &; 8 the temperature medium sent by the cooling - adsorption The desorption column, 12a, 12b is a second-way valve that has removed the gasoline vapor discharged from the first adsorption desorption column 11 and the second adsorption desorption column 16 through the second-way valve '13 system to adsorb the gasoline adsorbed by the first adsorption desorption column i As a getter pump for taking out the gasoline vapor from the first adsorption/desorption column 11, 14 is a pressurizing pump that pressurizes and compresses the air containing gasoline vapor taken out by the getter pump 13, and 15 is pressurized by the pressurizing pump 14. a third condensing device for liquefying and recovering gasoline by compressing the gas containing gasoline vapor, and a second adsorbing and desorbing tower for adsorbing and recovering the gasoline by the air containing gasoline vapor discharged from the third condensing device 15, 17a, 17b The flow regulating valve included in the first adsorption desorption column 11 and the second adsorption desorption column 16 is 18 for returning the liquefied gasoline to the gasoline piping of the gasoline storage tank 1, and the 19 series adjusting the third condensation device 15 and the second adsorption desorption A pressure controller for the pressure within the tower 16. The first condensing device 9, the second condensing device 10, and the first adsorption/desorption column 11 are arranged in order from the upstream side (front stage) of the flow of gasoline vapor to the downstream side (rear stage), and at the mounting position 2118-8326-PF 9 1327164 Laminated from the lower part to the upper part. Second, the description! The operation of the treatment and recovery device for gaseous carbon and chlorine in the figure. The operation of the device shown in the % state is performed in three steps of (4) attached #, the first-regeneration process, and the second regeneration process. First, the adsorption process is similar. The three-way reversing valve 33 is connected to the atmospheric discharge side, and the pressure regulating valve 4 is used to control the pressure of the gasoline storage tank to avoid the gasoline storage tank! The pressure exceeds the established pressure. When the oil supply is started, the three-way switching valve 3& switches to the recovery device side, and the two-way valve 12a is opened. Further, the three-way switching valve 3a is switched, and the gasoline tank or the like is transported to the gasoline storage tank via the gasoline pipe 2! When the oil supply starts, the gasoline vapor is stored in the gasoline storage tank. At this time, the > flying oil concentration of the gasoline vapor is about 30 to 40 v 〇 1% at a normal temperature. The gasoline vapor discharged from the gasoline storage tank is sent to the first condensing device 9 via the three-way switching valve 3a. The first condensing device 9 is indirectly cooled by the use of the liquid circulation system 8 to supply the temperature medium which has been cooled by the cold machine; In general, the first _ condensate: the internal is maintained from 〇t to about 5. 〇, #法制产, 5C, & oil money - part and the moisture contained in the gas condense, and use Luo, weeping eight μ anger, * use the rolling liquid separation Μ not shown) to separate into a gas h Oil gas) and liquid (gasoline). The liquid volume is stored on the lower side of the first condensation crack 9 and is sent to the gasoline storage tank via the gasoline piping 18. Further, in the first drawing, although the gasoline vapor is produced by the lower side of the first condensation device 9, The upper part of the condensing unit introduces gasoline vapor and flows downwards. The liquefied gasoline or water flows efficiently downward by gravity and airflow, and the recovery of these liquefied materials becomes easy. ...the pressure of the operating conditions of the first coagulation device 9 is O.IMPa, the cold portion/the degree of the dish 5 C. The gasoline vapor concentration becomes about Zhe. In addition,

2118-8326-PF 10 1327164 When investigating the saturated concentration of gasoline vapor, the saturated gasoline vapor concentration is about 20 vol% at a pressure of 0.1 MPa and a temperature of 51:. Under this condition, the gasoline vapor concentration is theoretically not lower than 20 vol%. Further, by lowering the temperature, the concentration of the gasoline vapor at the outlet of the first condensation device 9 can be lowered. However, when the set temperature is set below the freezing point, the water contained in the gas freezes in the first coagulation device 9, Since the pressure loss added to the inside of the first condensing device 9 is increased, the set temperature of the first condensing device 9 is preferably set to 〇 ° C to 5 ° C. Then, about 20 vol% of steam-oil vapor which cannot be processed by the first coagulation device 9 is supplied to the second coagulation device 1A. The second condensing device 10 is directly cooled by supplying the refrigerant cooled by the refrigerator 5 to the second condensing device 1 。. Generally, the inside of the first condensing device 1 is maintained at -2 〇. 〇到约—丨〇. 〇, one part of the gasoline helium is condensed and separated into gas (gasoline vapor) and liquid (gasoline). The liquid volume is stored on the lower side of the first condensing device 9, and is sent to the gasoline storage tank 1 via the gasoline dispenser 18. In addition, although the inside of the second condensing device i is cooled below the freezing point, because in the first condensing device 9 Most of the moisture is removed, so there is very little moisture in the second coagulation device 1 icing. Further, in the first drawing, although the gasoline vapor is made to flow from the lower side of the first condensing device 9, as in the case of the first condensing device 9, the gasoline vapor is introduced from above the second condensing device 10, and is downward. Circulating, and the liquefied gasoline or water flows efficiently downward by gravity and airflow, and the recovery of these liquefied materials becomes easy. On the other hand, the gasoline vapor concentration became about 8 vol% under the conditions of the operating pressure of the second condensing device of O.IMPa and the cooling temperature of 10 °C. In addition, when investigating the saturated concentration of gasoline vapor, the concentration of saturated gasoline vapor is about 8v〇1% at a pressure of 1Mpa and a temperature of io°c. Under this condition, the vapor concentration of steam 2118-8326-PF 11 1327164 is theoretically not Will be less than 8vol%. Further, the concentration of gasoline vapor at the outlet of the second condensing device 10 can be lowered by lowering the temperature. However, if the cooling is to -3, the gasoline vapor concentration is also about 5 vol%. It is known that even if it is cold, it is less than -3 (TC, the gasoline vapor concentration is hardly reduced. Because even if it is cold - it is low. Since the energy used in the 赃 is increased, the energy cannot be used efficiently. Therefore, the set temperature of the second condensing device 10 is set to exceed _3 (rc is preferable. Next, the second condensing device 10 cannot be used. About 8v〇1% of the steam and oil vapor to be treated is sent to the first adsorption/desorption column 11 for treatment. In the figure i, the first adsorption/desorption column 11 is operated as the adsorption column. Therefore, the two-way valve 12a is opened. (blackened), the flow rate adjusting valve 17a is in a closed state (blank). The adsorption tower is used as a desorption column after being subjected to adsorption treatment at an arbitrary timing. In this case, the two-way valve 12a is closed, and the flow rate adjusting valve 17a is It is used in the open state. The adsorbent for adsorbing gasoline vapor is sealed in the first adsorption desorption column 11. The adsorbent of the sulphur oil vapor is made of Shishijiao, especially having a pore diameter of 4~1 〇〇 之·石石胶 or synthetic zeolite. Monomer or a mixture of these Effectively, the gasoline component is adsorbed and removed by passing the gasoline vapor through the adsorbent, and becomes a clean air of less than 1 vol% of the gasoline concentration, and is discharged to the atmosphere via the second-way wide 12a. • The first adsorption desorption The column 11 is independent of the function of adsorption and desorption of the gasoline vapor. 'Always the temperature medium supplied by the liquid circulation pump 8 is cooled to a fixed temperature. That is, the cooling system for the first condensation device 9 and the first adsorption desorption column 11 is always The operation control is performed in such a manner that the temperature of the set system is maintained at 〇 5 ° C. This is because the silicone resin filled in the first adsorption/desorption column 11 is exchanged by heat from the fin tube 2118-8326-PF 12 , the parent exchanger or the like. The heat transfer of the device (not shown) is cooled, so a certain amount of cooling time is necessary and indispensable, and it is not possible to operate between (4). In addition, it can be cooled in a short time to include cooling performance. Machine 5, has a bad impact on equipment costs, because it can not provide cheap gasoline recovery equipment f In addition, by reducing the first adsorption desorption tower i (internal temperature, and increase the capacity) can be reduced (four) use However, when the internal temperature of the first adsorption desorption column 11 is changed to below the freezing point, since the water is frozen in the first adsorption desorption column η and the ice is gradually stored in the adsorbent such as ♦, the adsorption of the adsorbent occurs. The performance reduction handle sighs the problem of the reduction of the king, therefore, it is preferable to set the internal temperature of the first adsorption desorption tower to be above the freezing point. From the above, by having the first condensation device 9 and the first adsorption desorption tower The cooling system of the cooling system of 11 and the cooling system of the second condensing device 1 are different in temperature, and the gasoline can be efficiently recovered. The first adsorption desorption column 11 adsorbs atmospheric gas, although the first adsorption desorption column 11 The shape of the external structure is not limited, but since the pressure inside the adsorption tower becomes about MPa02 MPa at the time of desorption, a cylindrical structure is employed. By using the cylindrical structure, the pressure acting on the wall surface can be made uniform, and even if the pressure in the adsorption tower becomes about 0.02 MPa, the safety can be high, that is, the adsorption desorption tower such as shape deformation does not occur. Further, regarding the internal structure of the first adsorption desorption % 11 'considering the heat conduction to the Shiqi gum or the synthetic zeolite, the fin tube heat exchanger is arranged (the heat sink is used to make the temperature medium flow guide the heat pipe), and the Shixia gum or The synthetic zeolite is inserted between the aluminum fins, and at the same time, the silicone outflow is provided on the upper and lower sides to prevent the net from 'preventing the silicone to flow out to the pipe' and to improve the flow of the gas. In this case, in order to make the adsorption of the rubber vapor to the gasoline vapor uniform, a rectifying plate made of a punched metal plate or the like may be provided to uniformly flow the gasoline vapor to the first suction 2118-8326-PF 13 1327164 with the desorption column 11 . The direction of the heat pipe of the fin tube is set to be parallel with the flow of steam and gas, so as to avoid the pressure loss when the gasoline vapor flows. . . . 'In order to efficiently cool the filling near the outer wall (4) It is necessary to make a gap between the heat exchanger of the tab tube and the outer wall. ' 纟 情况 ' 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉 藉Excellent K copper is optimal, combined with the length of the heat sink itself for the non-bending side extension tab (4), and is effective for eliminating the gap between the outer wall and the tube heat exchanger. Also, • To eliminate the outer wall The gap between the heat exchanger and the heat exchanger can also be made into a metal rod or a tube having a heat sink, etc. Further, in the case where the temperature medium flows to the heat pipe of the fin tube heat exchanger, the heat pipe is inserted into the heat pipe. The piping for flowing the temperature medium is branched, and the fin tube heat exchanger is divided into a plurality of groups, so that the temperature medium flows in parallel. Therefore, the piping of the temperature medium flowing can be reduced, and the temperature medium can be lowered. for The capacity of the liquid of the first adsorption desorption tower is the following. In addition, in this example, since the gasoline vapor flows from the bottom to the top, the reaction is placed into a fin tube heat exchanger and the lower portion of the silicone outflow prevents the mesh from coming into contact. Preferably, the space can be eliminated between the silicone outflow prevention net and the tab tube heat exchanger, that is, the space filled only with the silicone rubber can sufficiently cool the silicone rubber during adsorption. As a result, the gasoline at the lowest concentration of gasoline can be prevented. The temperature of the Shiqi gum in which the vapor flows in is increased, and the first adsorption desorption column 11β which is safe can be provided. In addition, in the case where the gasoline vapor flows from the top to the bottom, of course, the upper silicone outflow prevention net and the tab tube heat exchanger In the case where the first condensing device 9 and the second condensing device 10 are not disposed in the first stage of the first adsorption/desorption column 11, the high-concentration gasoline vapor flows into the first suction 2118-8326-PF 14 1327164 with the desorption column 11 and is adsorbed. The agent adsorbs the moisture contained in the gasoline vapor, and the adsorption performance of the gasoline vapor is lowered, and the amount of the adsorbent is required to be exceeded. Further, the temperature of the first adsorption desorption column 11 is lowered. In the case of freezing below, the moisture " icing on the surface of the adsorbent may cause a large failure such as full of gas. In the present embodiment, the first condensation device 9 and the second condensation are disposed in the first stage of the first adsorption/desorption column 11 Since the device 10 is removed together with the gasoline vapor, the influence of the moisture in the first adsorption/desorption column 11 can be prevented. Further, since the amount of gasoline processed in the first adsorption/desorption column 11 can be greatly reduced, The first adsorption/desorption column 11 is made smaller, and can be produced inexpensively. Further, in the present embodiment, since the first concentration device 9 can be used to reduce the high concentration (40 vol%) of gasoline discharged from the gasoline storage tank 1 to 20 vol%. Therefore, the second coagulation device 1 can be lowered to 8 vol. / ◦, so the amount of gasoline processed in the first adsorption/desorption column 11 can be reduced to 20 / 〇 (-8% / 40%) of the total intake amount. Namely, the volume of the first adsorption/desorption column 11 can be set to about 1/5 by providing the first condensation device and the second condensation device 1 in the first stage of the first adsorption-desorption column 1 . • Next, the influence of the cooling temperature of the second condensing device 10 on the amount of mash filling of the first adsorption/desorption column 11 will be explained. Fig. 2 shows the inside of the second coagulation device 10. The relationship between the cooling temperature of the crucible and the amount of the gel filling required for the case where the gasoline vapor concentration becomes 1 vol% or less at the outlet of the first adsorption/desorption column 11. Further, Μ is based on the amount of glue required for the case where the cooling temperature of the second condensing device 10 is 5t:, which indicates the amount of sputum reduction. So by lowering the second condensation

The cooling temperature of the apparatus 10 is such that the amount of the yttrium filled in the first adsorption desorption column i 1 is changed. However, it was found that even if it was cooled to a 30. (The following amount of silicone is also a few.) Salty. For the results of experimental investigations on various gasolines, it is known that the composition of gasoline vapor 2118-8326-PP 15 1327164 is irrelevant, even if the cooling temperature becomes below 30 °C, gasoline vapor The fact that the saturation concentration is hardly lowered is also due to the decrease in the amount of reduction of the silicone rubber. Therefore, in consideration of the input energy, it is not high efficiency to set the cooling temperature of the second condensation device 10 to _30 乞 or less. The cooling temperature of the second condensation-device 10 is set to a 30T: preferably. 'Next' describes the regeneration process of the first adsorption-desorption column 11, that is, the desorption process of the gasoline. Vapor. The regeneration of the first adsorption-desorption column π The process includes: a first regeneration process 'desorbing gasoline from the first adsorption desorption column 11 and discharging it to the atmosphere via the second condensation device 15 and the second adsorption desorption column 16; and a second regeneration process, desorbing by the second adsorption The tower 16 desorbs the gasoline and discharges it to the atmosphere via the first condensing device 9, the second condensing device 10, and the first adsorption desorption column 11. First, the first regeneration process will be described. In the case where the adsorbed gasoline is desorbed, the gas is sucked by the first adsorption/desorption column 11 through the three-way switching valve 3b by the getter pump 13 and the gasoline is desorbed by the adsorbent. At this time, the two-way wide 12a is closed. When the pressure in the adsorption desorption column 11 is reduced to a predetermined pressure, the flow regulating valve is opened. 17a 'The fixed flow of air flows from the atmosphere into the first adsorption desorption column U, and the pressure inside the first adsorption desorption column u becomes a substantially constant value. Although the first adsorption desorption column operates at an atmospheric pressure of 〇1 MPa during adsorption, since it is depressurized to below atmospheric pressure by the getter pump 13 during desorption, the gasoline adsorbed by the adsorbent is concentrated by the pressure difference. In the case of a high concentration of the state solution and in this case, although it is related to the gas flow rate of the gasoline vapor or the adsorption at the time of adsorption, the pressure in the first adsorption desorption column U is controlled to be 〇·〇2~〇. 〇4MPa' and the gasoline vapor concentration can be changed to 2〇~4〇v〇1%. The desorbed gasoline vapor is led to the pressure pump via the three-way selector valve 3c to the pump 2118-8326-PF 16 1327164 14 ° Pump 14 will The oil vapor is pressurized to about 0.3 MPa and supplied to the second condensing device 15. That is, the gasoline concentration of 30 vol%, the pressure 〇3 MPa, and the pressurized gasoline vapor are supplied to the third condensing device 15. By using the liquid. 8 is supplied to the temperature medium cooled by the refrigerator 5 to indirectly cool the third condensation device 15. Generally, the third condensation device 15 is internally held in a portion of the gasoline vapor from 〇r ' to about 5. The moisture is condensed, and is separated into a gas (gasoline vapor) and a liquid (gasoline) by a gas-liquid separator (not shown) or the like, and is stored in the lower side of the third condensing device 15, and is sent back via the gasoline_pipe 18. To the petrol storage tank 1. Further, as shown in Fig. 1, by introducing gasoline vapor from above the second condensing device 丨5 and flowing downward, the liquefied gasoline or water flows efficiently downward by gravity and airflow, and these liquefied materials are liquefied. The recycling becomes easy. On the other hand, the pressure of the operating conditions of the third condensing device 15 is 0.3 MPa and the cooling temperature is 5. . Under the condition, the gasoline vapor concentration at the outlet becomes about 8 vol%. In addition, from the saturation concentration curve of gasoline vapor, the saturated gasoline vapor concentration is about 8v〇1% at a pressure of 0.3MPa and a temperature of 5°C. In this article, the π oil vapor concentration is theoretically not lower than 8v〇1%. X, by lowering the temperature, the concentration of gasoline vapor at the outlet of the third condensing device 15 can be lowered. However, when the set temperature is set to be below the freezing point, the water contained in the gas is frozen in the third condensation device 15, because the pressure loss inside the third condensation device 15 is increased, so the second condensation device 15 The set temperature is preferably set from ot to about rc. Further, in the second coagulation device 15, since it is pressurized to about 3 MPa, a cylindrical structure is employed. By adopting the cylindrical structure, the pressure acting on the wall surface can be changed to a uniform sentence 'even if the third condensing device i...the pressure becomes about 0.3 MPa', the safety can be high, that is, the second deformation does not occur, etc., 2118-8326 - PF 17 1327164 Three condensation device 15. Then, about 8 vol% of the vapor vapor which cannot be treated by the third condensing device 15 is sent to the second adsorption/desorption column 16 and processed. Fig. 1 shows a case where the second adsorption/desorption column 16 operates as an adsorption column. Therefore, the two-way valve 12b is opened (blackened), and the flow regulating valve 17b is in a closed (blank) state. The adsorption tower is used as a desorption column after being subjected to adsorption treatment at an arbitrary timing. In this case, the two-way valve 12b is closed and the flow regulating valve i7b is in an open state. The second adsorption-desorption column 16 is also sealed with an adsorbent for adsorbing gasoline vapor, which is the same as the first adsorption-desorption column 11. The gasoline vapor is passed through the adsorbent to adsorb and remove the gasoline component, and becomes clean air having a vapor concentration lower than 丨v〇1%, and is discharged to the atmosphere via the two-way valve 12b. Further, the first adsorption/desorption column 16 is also cooled to a fixed temperature by the temperature medium supplied from the liquid circulation pump 8 regardless of the function of adsorption and desorption of the gasoline vapor. That is, it is always kept 〇~5 like the first adsorption desorption column U. The operation mode is controlled by the method of 〇. Further, the second adsorption/desorption column 16 is subjected to pressure by a pressure of about 0.02 MPa in the gas inside the adsorption column when the adsorption pressure is about 0.3 MPa. Therefore, a cylindrical structure is employed. By adopting the cylindrical structure, the pressure acting on the wall surface can be made uniform, and even if the pressure in the first adsorption/desorption column 16 is varied from 〇〇3 to about M3 Mpa, safety can be achieved, that is, the shape does not occur. a second adsorption desorption column 16 such as a deformation. Further, regarding the internal structure, the same configuration as that of the first adsorption desorption column is preferable. According to the above, in the first regeneration process, the gasoline vapor discharged from the first adsorption desorption column can be efficiently liquefied and recovered by performing the cold portion and adsorption in a pressurized state. Further, at the time of desorption, although the temperature inside the first adsorption desorption column u is raised by raising 2118-8326-PF 18 1327164, the desorption rate can be increased, or the a-oil vapor concentration can be increased, but the temperature is varied and consumed. The energy is increased, so the temperature is not increased during desorption, and the same temperature as that at the time of adsorption is used to solve the problem, which is effective for energy saving. 'Secondary' illustrates the second regeneration process in which the gasoline is desorbed by the second adsorption/desorption column 16, and is discharged to the atmosphere by the first condensation device 9, the second condensation device 1, and the first adsorption desorption column 11. In the case where the gasoline adsorbed by the adsorbent in the second adsorption desorption column 16 is desorbed, the gas is sucked from the second adsorption desorption column 16 by the getter pump 13 via the 'φ three-way switching valve 3b and is adsorbed by the adsorbent. Gasoline is desorbed. At this time, the two-way valve 12b is closed. Further, when the pressure in the second adsorption/desorption column 16 is lowered to a predetermined pressure, the flow rate adjusting valve i7b is opened, and the air of the fixed flow rate flows from the atmosphere into the second adsorption/desorption column 16, and the pressure inside the second adsorption/desorption column 16 becomes Approximate setting. Although the second adsorption/desorption column 16 operates at an atmospheric pressure of 0.3 MPa during adsorption, since it is depressurized to below atmospheric pressure by the getter pump 13 during desorption, the gasoline adsorbed by the adsorbent is concentrated to a high level by the pressure difference. The state of concentration is desorbed. In this case, although it is related to the gas flow rate of the gasoline vapor or the adsorption amount at the time of adsorption, 'but by controlling the pressure in the second adsorption desorption column 16 to 0. 〇 2 to 0.04 MPa, the gasoline vapor can be made. Degree becomes 2〇~4〇vol%. • The desorbed gasoline vapor is led to the first condensation device 9 via the three-way selector valve 3c. That is, a gasoline concentration of 30 vol%, a high concentration of pressure 〇1 MPa, and gasoline vapor are supplied to the first condensing device 9, and as described above, the inside of the first condensing device 9 is maintained at from 0 ° C to about 5 ° C. One part of the gasoline vapor and the moisture contained in the gas are condensed, and are separated into a gas (gasoline vapor) and a liquid (gasoline) by a gas-liquid separator (not shown) or the like. Next, the first coagulation device 9 cannot supply about 20 vol% of gasoline vapor at 2118-8326-PF, and the second coagulation device 10 is supplied in the same manner as the time. Here, the liquefaction enthalpy is further carried out - ^" only about 8% of the gasoline vapor-adsorption desorption column u which cannot be treated by the second coagulation device 10, by the gasoline second-adsorption desorption column U. The gasoline component is adsorbed and removed by the adsorbent, and the clean air having a low gasoline concentration of 1% is obtained, and is discharged to the atmosphere via the two-way valve 12a. As described above, by performing the adsorption process, The first regeneration process, and the first regeneration process, and the series of operations are completed, each time the oil storage tank i is supplied with oil, the series of operations are repeated. With this action, only a maximum of 1 v is discharged to the atmosphere. 〇i% of gasoline vapor is a treatment and recovery device for gaseous hydrocarbons with a small environmental load. Moreover, because only the most gasoline vapor is discharged, it can recover 40% of the gasoline vapor of 40v〇1%, and the recovery efficiency It is 97.5%, which is a highly efficient recovery device. Moreover, since the adsorption operation is performed after the condensation operation in one temperature zone, the first adsorption/desorption column 11 can be greatly miniaturized, and the device can be made small overall. Chemical Further, 'the discharge port of the gasoline vapor from the first adsorption desorption column u and the second adsorption desorption column 16 at the time of desorption is formed, and the gasoline of the first adsorption desorption column 11 and the second adsorption desorption column 16 disposed at the time of adsorption is formed. The supply port of the vapor concentration is in the same portion. Since the adsorption desorption columns U and 16 are used in such a manner that the concentration of the gasoline vapor at the outlet of the adsorption desorption columns u and 16 becomes less than 1 vol%, they become gasoline in the adsorption desorption columns ii, 16 at the time of adsorption. In the vicinity of the vapor inlet, the gasoline vapor is densely adsorbed, and the gasoline vapor is less adsorbed in the vicinity of the gasoline vapor discharge port of the adsorption/desorption columns 11 and 16. In order to efficiently collect the adsorption/desorption column 11 by coagulation during desorption, 16 discharged gasoline vapors 'requires as much as possible to increase the concentration of gasoline vapor. Therefore, because high-density absorption of 2118-8326-PF 20 1327164 ::: can be discharged from gasoline vapor can discharge high concentrations of gasoline vapor, so the density is south. The part that adsorbs the gasoline vapor, that is, in the vicinity of the adsorption desorption and extraction, and the oil vapor suction port, and in the desorption, the exhaust steam is only relied on the pressure of _W 13 The desorption method is effective because it is not used to flush the gas system from the outside, and in this embodiment, it is also replaced by a gas which is inhaled and used with a flushing gas from the adsorption desorption columns 11, 16. The gasoline vapor is desorbed. In the present embodiment, the air is sent to the atmosphere of the flushing gas system of the adsorption desorption columns 11 and 16. Since the air contains a certain amount of water, the flushing gas supplied to the adsorption desorption columns u and 16 is required. As described above, as shown above, when the pressure in the adsorption/desorption columns 11, 16 is lowered to a predetermined pressure after a certain period of desorption, the flow rate adjusting valves m, 17b are opened, and the air of a fixed flow flows in from the atmosphere. The adsorption/desorption columns u and 16 are desorbed so that the pressure inside the adsorption desorption columns u and 16 becomes a substantially constant value. The figure is a diagram for explaining a method of controlling the amount of gas for flushing. By this means, it is possible to prevent the amount of the inhaled gas from decreasing as time passes, and the desorption operation of the gasoline vapor can be stably performed. As a timing of introduction of the rinsing gas, there is a method of introducing a rinsing gas after a fixed time from the desorption by a timer or the like (timer method), and introducing the rinsing when the internal pressure of the adsorption/desorption columns 11 and 16 reaches a set value. The method of the gas (pressure measurement method) and the method of introducing the gas for flushing (gas amount measurement method) when the gas amount of the gasoline vapor discharged from the adsorption desorption columns u and |6 reaches a set value. Although the timer method is most advantageous in terms of initial cost, the timing of introducing the flushing gas is shifted according to the amount of gasoline adsorbed by the adsorption desorption columns 1^, 16 and may reduce the effective introduction of the flushing gas 2118-8326-PF. 21 ^27164 : If the amount of adsorption is large, the amount of gas in the gasoline vapor will be reduced in the adsorption desorption "I. If the amount of adsorption is small, the amount of gasoline discharged from the /6 is less in the mountains, and the adsorption desorption tower 11 is 16 The time zone in which the amount of gasoline vapor gas is reduced is increased, and the amount of gasoline desorption tower is reduced by the amount of the adsorption desorption tower. The method of gas pumping and gas efficiency is as follows: 1. The problem of the above-mentioned timer mode is determined, and In addition, in this gasoline recovery unit, in terms of safety, it is indispensable to install a pressure gauge system for the ^= flow piping system. Therefore, the :::= test method can be combined with (four) pressure gauges, so in three types In the middle of the system, the oil supply to the gasoline storage tank of the gas station is regularly carried out, and the oil vapor in the production line is limited to the fixed time of the day. Point of view in producing gasoline When the vapor is to be subjected to the adsorption operation, and the regeneration of the desorption columns U and 16 is carried out in the time zone when the gasoline vapor is not generated, this is effective. Secondly, the number of gasolines which are reduced by the amount of gas and long-time operation is used. Therefore, it is known that the recovery rate is lowered by reducing the amount of gas. It is also known that when the gas flow rate becomes 40 L/min or more, the recovery rate does not increase. This is because the flow rate is increased when the flow rate of the wide body is increased. The amount of air flowing into the regulating valve 17a is increased: = the oil vapor concentration is diluted by the air and lowered in the gasoline condensation of the third condensing device 15. Therefore, it is known that the steam is removed by the first adsorption desorption tower In the case of vapor desorption, it is preferable that the gas flow rate is at most 4 〇L/min, and it is possible to efficiently recover the first adsorption/desorption column U by a long time at a low flow rate. The method of controlling the hydrocarbon-like hydrocarbon and the recovery device 2118-8326-PF 22 1327164. When the recovery device is stopped, the suction pump 13A pressurizes the pump 14 to stop. The two-way valves 12a and 12b are fully closed. And traffic ^ The adjustment valve is deuterated and 17b is in a closed state. The first adsorption desorption column U and the second and desorbing column 16 are cooled by the temperature medium cooled by the refrigerator 5. When t/fly/the storage tank 1 starts to supply oil The three-way switching valve 3a is switched 'and the -way valve 12a is opened, and the cooling of the second condensing device 10 is started. The second condensate<- sigh,, σ 裒 is set to 1 〇 when the internal temperature reaches the set value, the gasoline The recovery of the steam begins. At the end of the supply of the gasoline storage tank i and the generation of the gasoline vapor, the three-way selector valve 3a is switched, and the second passage 12 a is closed, the second condensation device is stopped! 0 the cooling is stopped. Then, two When the gate valve 2 b is opened and the getter pump 13 and the pressurizing pump 14 are operated, the gasoline vapor is desorbed by the first adsorption desorption column 11 and passed through the third coagulation device 15 and the second adsorption desorption column 16 The atmosphere is discharged. At this time, when the pressure in the first adsorption desorption column is reduced to a predetermined pressure by the operation of the getter pump 13, the flow rate adjusting valve 17a starts to open, and the flow rate adjustment is controlled in such a manner that the flow rate flows to the first adsorption desorption column 11 at a predetermined flow rate. The opening degree of the valve 17a. At the end of the first regeneration process, the intake pump 13 or the pressure pump 14 is stopped, and the flow rate adjustment valve 17a is turned off, and the two-way valve 12a is turned off. Then, the cooling of the first condensing device 1 is started, and when the temperature inside the second condensing device 达到 reaches the set value, the regeneration of the second adsorption/desorption column 16 is started. When the two-way valve 12a is opened and the suction pump 13 and the pressure pump 14 are operated, the gasoline vapor is desorbed by the second adsorption/desorption column 16, according to the first condensation device 9, the first condensation device 10, and the first adsorption. The order of the desorption column π is discharged through the backward large rolling. At this time, when the pressure in the second adsorption/desorption column 16 is reduced to a predetermined pressure by the operation of the getter pump 13, the flow rate adjusting valve i7b starts to open, and the flow rate adjustment is controlled in such a manner that a predetermined flow rate flows to the second adsorption/desorption column 16. 2118-8326-PF 23 1327164 Opening of valve 17b. At the fixed time, when the regeneration process is completed, the cooling of the second coagulation device 10 is stopped and the intake pump 13 or the pressurizing pump 14 is stopped, the two-way valves 12a and 12b are fully closed, and the flow rate adjusting valves 17a and 17b are closed. status. In the above manner, the recovery device is repeatedly operated. Finally, the effect of increasing the internal pressure of the second coagulation device 15 and the second adsorption desorption column 16 by using the pressurizing pump 14 and the pressure controller 19 will be described. Fig. 5 is a view showing the relationship between the internal pressure of the third condensing device 15 and the second adsorption/desorption column 16 and the adsorbent charged in the second adsorption/desorption column 16. Thus, it is known that the amount of the silicone filler can be reduced by increasing the internal pressure. However, it is found that even if it becomes higher than 〇 4 MPa, the amount of the silicone filler is hardly reduced. On the other hand, when the pressure is increased, the pressure of the third condensing device 15 and the second adsorption/desorption column 16 needs to be increased, and the device becomes expensive. Therefore, it was confirmed that the internal pressures of the third condensing device 15 and the second adsorptive desorption column 16 were set to 〇·2~0·3ΜΡα. Further, Fig. 6 is a view showing an overall configuration of a flow of a treatment and recovery apparatus that does not include gaseous hydrocarbons of the pressurizing system 14 and the pressure controller 19. Thereby, the number of components constituting the device can be reduced. Since the amount of the silicone used in the second adsorption/desorption column 16 is twice or more, the second adsorption/desorption column 16 becomes large, and the device cost is not lowered. From the above matters, 'the pressure pump 14 and the pressure controller 19 are provided, and the internal pressures of the third condensing device 15 and the second sorption desorbing tower 16 are raised, and by two to 0.4]\^3, preferably 〇 .2~〇.31^?&, and has the effect of providing an inexpensive recycling device. (Second Embodiment) Fig. 7 is a view showing an overall configuration of a flow of a gaseous hydrocarbon processing and recovery apparatus according to a second embodiment of the present invention. 2118-8326'ρρ 24 1327164 The difference between the second embodiment and the first embodiment is that the two-way switching valve 3a is not used. In the second embodiment, as shown in Fig. 7, the three-way switching valve 3a is not required, and the valve 21 is newly included. In such a configuration, the pressure loss in the recovery device is smaller than the set value of the pressure regulating valve 4, and generally, in the case where the gasoline vapor flows to the recovery device and the gas is blocked in the recovery device, etc., it is automatically The gasoline vapor is discharged to the atmosphere via the pressure regulating valve 4. In addition, the recovery apparatus of the second embodiment can reduce the amount of adsorbent used by the condensation of two temperature zones, because the pressure loss of the recovery device can be reduced to the limit. Implement this device. Therefore, the gas in the recovery device and the gas storage tank 1 are not higher than the set value of the pressure regulating valve 4, and the safety recovery device can be improved. (Embodiment 3) FIG. 8 is a view showing an overall configuration of a flow of a gaseous hydrocarbon processing and recovery apparatus according to a third embodiment of the present invention. In the first embodiment, the air suction pump 13 and the squeezing pump 14 are continuously provided. However, in the third embodiment, the pressure buffer container 31 and the pressure measuring device 32 having the 岐 volume are provided in the suction. Between the air pump 13 and the pressurized pump 14, the pressure between the intake system η and the pressure pump 14 is monitored, and the malfunction of the operation of the air suction pump 13 and the pressure pump 14 can be detected, and the operation of the danger can be prevented. . That is, the pressure between the getter pump 13 and the pressurizing pump 14 becomes a negative pressure to prevent the performance of the pressurizing pump 14 from deteriorating, and the pressure between the getter pump 13 and the pressurizing pump 14 becomes a positive pressure. The situation can prevent the performance of the getter pump from degrading. Further, by including a space of a fixed volume between the getter pump 13 and the pressurizing pump 14, the intense pressure fluctuation can be alleviated, and the running difference 2118-8326-PF 25 丄 w/164 can be detected. Thereby, the desorption process from the adsorption/desorption column 11 in the recovery device can detect the malfunction of the getter pump 13 or the pressurizing pump 14, and can prevent the rapid expansion without a rapid increase, and can provide a safe recovery device. effect. [Fourth Embodiment] Fig. 9 is a view showing an overall configuration of a flow of a treatment and recovery apparatus in a gaseous hydrocarbon gas according to a fourth embodiment of the present invention. The difference between the fourth embodiment and the first embodiment is that the flow of the gas treatment at the time of regeneration of the first absorption/desorption column 11 is different, that is, the second regeneration process shown in the first embodiment is different. Further, in the fourth embodiment, as shown in Fig. 9, the two-way switching valve 3c is not disposed between the air suction pump 丨3 and the pressure pump 14, but is disposed in the third condensing device 15 and the second adsorption desorption Between towers 16. Further, the pressure controller 19a for adjusting the pressure in the second adsorption/desorption column 16 is additionally provided with a pressure controller 19b for adjusting the pressure in the third coagulation device 15. In the first embodiment, the gasoline vapor desorbed by the second adsorption/desorption column 16 by the intake pump 13 is supplied to the first condensing device 9, and is discharged to the atmosphere through the second condensing device 10 and the first adsorption/desorption column 11. However, in the fourth embodiment, the second adsorption/desorption column 16 is pressurized by the pressurized system 14 by the A oil vapor desorbed by the intake pump 13, and then supplied to the third condensation device '15. Then, the gasoline vapor passing through the third condensing device 15 passes through the second condensing device 10 and the first adsorption/desorption column 11 and is discharged to the atmosphere. By making such a flow, the pressurizing pump 14 can be effectively utilized, and the gasoline vapor passing through the third coagulation device 15 can be efficiently recovered. Further, in the case where the evaporation temperature of the refrigerant of the cold beam machine 5 cannot be lowered, it is effective to use such a flow, and the effect of efficiently recovering gasoline with 2118-8326-PP 26 can be obtained. (fifth embodiment) FIG. 10 is a view showing an overall configuration of a gas-like carbon gas external treatment and recovery apparatus according to a fifth embodiment of the present invention. The difference between the fifth embodiment and the i-th embodiment is that the flow of the gas treatment at the time of regeneration of the first adsorption/desorption column 11 is different, that is, the first regeneration process shown in the first embodiment is different. In the i-th embodiment, the second adsorption/desorption column 16 is disposed after the third condensation device i5 as in the first embodiment, and in the fifth embodiment, as shown in the first figure, in the third embodiment. The subsequent section of the coagulation through 15 includes a gas storage container 41. Further, 42 is a flow rate adjusting valve provided as a main flow controller between the gas storage container 41 and the three-way switching valve 3b, and 43 is disposed between the gas storage container 41 and the third condensing device 15 Flow valve. In the first embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption tower is pressurized by the pressure pump 14, and then supplied to the third condensation device 15. The gasoline vapor passing through the third condensing device 15 is passed through the second adsorption/desorption column 16 and then discharged to the atmosphere. However, in the fifth embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption column 11 is pressurized by the pressure pump 14, and then supplied to the third condensation device 15. Although it is the same as the first embodiment, the gasoline atmosphere by the third condensing device 5-1 is directly cooled by the gas storage container 41 and sealed in a state of pressure compression. When the pressure of the gas storage container 41 reaches a predetermined pressure, the first regeneration process ends. Then, the gasoline vapor stored in the gas storage container 41 is supplied to the first adsorption/desorption column i via the flow rate adjusting valve 42, and the gasoline vapor is removed by the adsorbent in the first adsorption/desorption column 11 and then discharged to the atmosphere. By constructing the 2118-8326-PF 27 1327164 configuration and processing flow, the system configuration can be simplified and the cost of the device can be reduced. Further, the operation time of the getter pump 13 and the pressurizing pump 14 can be reduced, and energy can be saved. According to the above, the effect of providing the energy-saving recovery device at a low cost by including the cartridge storage container 41 in place of the second adsorption/desorption column 16 is described. FIG. 11 is a view showing the first aspect of the present invention. (6) Overall structural diagram of the flow of the gas-like hydrocarbon in the embodiment and the processing and recovery device. The difference between the sixth embodiment and the second embodiment is that the flow of the gas treatment during the regeneration of the first adsorption/desorption column 11 is different, that is, the first regeneration process shown in the second embodiment is different and there is no second. Recycling process. Further, in the first embodiment, as shown in the first embodiment, the inside of the third condensing device 15 is cooled to 〇 rc by the temperature medium. However, in the sixth embodiment, as shown in FIG. It is shown that the fourth condensing device 51 which is directly cooled by the refrigerator 5 by the refrigerant is formed, and the second adsorption/desorption column 16 is not required. In the first embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption column 11 is pressurized by the pressure pump 14, and then supplied to the third condensation device 15. The gasoline vapor passing through the third condensing device 15 is passed through the second adsorption/desorption column 16 and then discharged to the atmosphere. However, in the sixth embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption column 11 is pressurized by the pressure pump 14 and supplied to the fourth condensation device 51. The inside of the fourth condensing device 51 is directly cooled by the refrigerant cooled by the cold beam machine 5 to become about 3 〇 ° C. At a pressure of 0_3 MPa and a cooling temperature of -3 (the condition of rc, the gasoline vapor concentration becomes about 1 vol%. Therefore, it is directly discharged to the atmosphere. Thereby, the cost of 2118-8326-PF 28 1327164 can be simplified. Further, the second regeneration system is not required. The operation time of the pump 14 can save the energy system structure and reduce the number of devices. The air suction pump 13 and the pressure source can be reduced. The fourth condensation device 51 has the above effect. The seventh embodiment Recycling equipment capable of providing energy saving at a low cost by including an alternative to the third condensing device 15

Fig. 12 is a view showing the overall configuration of a flow of a process and a recovery apparatus for a gaseous carbon gas according to a seventh embodiment of the present invention. The difference between the seventh embodiment and the first embodiment is that the third adsorption/desorption column 61 having the same size and size as the first adsorption/desorption column i i is formed in parallel, and the second adsorption/desorption column 16 is not required. Namely, the gasoline vapor discharged from the second condensation device 1 is adsorbed in the first adsorption/desorption column 11, and the gasoline vapor adsorbed by the third adsorption/desorption column 61 is analyzed to be different. In Fig. 12, the 61 series specification is the same as the first adsorption desorption column u, and the third adsorption desorption column, 62a, 62b, is included in parallel with the first adsorption desorption column 11, and is used to be used by the second condensation device i. The discharged gasoline vapor is introduced to the adsorption valve of the first adsorption/desorption column 11 or the second adsorption/desorption column 16, and 63a, 63b are desorbed when the gasoline vapor is desorbed by the first adsorption/desorption column u or the getter pump 13 The valves '64a, 64b are used to discharge the gasoline vapors processed by the first adsorption desorption column 11 or the third adsorption desorption column 61 to the atmosphere, and the exhaust valves '65a, 65b are connected to the first adsorption desorption column π or When the three adsorption/desorption column 61 desorbs the gasoline vapor, a gas flow rate adjustment valve for introducing air into the first adsorption/desorption column 11 or the second adsorption/desorption column 61 is introduced. 2118'8326-PF 29 1327164 Next 'Description of action. The apparatus shown in the seventh embodiment is generally carried out in accordance with the steps of the adsorption process and the regeneration process (four). First, the second attachment process is described. When the fuel supply is started, the three-way reversing chamber 3a is switched to the recovery device: after the switching of the two-way switching valve 3a, the tanker or the like starts to the storage tank 1 via the gasoline piping 2 When the oil is supplied, the gasoline vapor/flying oil storage tank 1 filled with the gasoline storage tank i is discharged. At this time, the gasoline vapor concentration is about 30 to yang at room temperature. 1%. The gasoline vapor discharged from the gasoline storage tank 1 is supplied to the first condensing device 9 via the three-way switching enthalpy 3a'. The first condensing device 9 is cooled by the liquid circulating medium 8 to be cooled by the liquid circulating pump 8 and cooled by the ground. Generally, the inside of the first condensing device 9 is kept at about, and a part of the gasoline vapor and the moisture contained in the gas are condensed, and separated into a gas (gasoline vapor) and a liquid (gasoline) by using a gas-liquid separator (not shown) or the like. The liquid volume is stored on the lower side of the first condensing device 9, and is sent to the sputum storage tank 1 via the gasoline pipe 18. Next, about 20 v 〇 1% of the steam vapor which cannot be processed by the first condensing device 9 is supplied to the second condensing device 1 〇. The second condensing device 1 is directly cooled by supplying the refrigerant cooled by the refrigerator 5 to the second condensing device 1 。. Generally, the inside of the second condensing device 10 is maintained from -2 〇〇 c to about _ 1 (rc, part of the gasoline vapor is condensed, and separated into gas (gasoline vapor) and liquid (gasoline)' to discharge only uncondensed gasoline. The volume of the vapor β liquid is stored in the lower side of the first condensing device 9 and is sent to the gasoline storage tank 1 via the gasoline piping 18. Further, in the first embodiment, when the gasoline vapor discharged from the gasoline storage tank 1 is adsorbed, Since the desorption operation is not performed, the second coagulation device 10 is stopped at the end of the adsorption operation. However, in the seventh embodiment, when the gasoline vapor discharged from the gasoline storage tank 1 is adsorbed, the other adsorption solution 2118 is also used. -8326-PF 30 1327164 The suction tower performs the desorption operation of the gasoline vapor, so the cooling of the second condensing unit 1 is not stopped when the recovery is performed. Next, about 8 vol% which cannot be processed in the second condensing unit 1 The steam is sent to the adsorption desorption column 1 to be treated by steam. In Fig. 12, 11 is shown as the adsorption column and 61 is operated as a desorption column. Therefore, the adsorption valve 62a is opened (blackened), 62b. In the state of being closed (blank), it is used as a desorption column after being adsorbed at an arbitrary time as an adsorption tower. In this case, the adsorption valve 62a is closed and 62b is opened, and the desorption of gasoline is completed. The time is 're-used as an adsorption tower, and the operation is repeatedly used in time. The switching of adsorption and desorption is controlled by the switching of the adsorption valves 62a and 62b, and is sealed in the adsorption/desorption columns u and 61. An adsorbent that adsorbs gasoline vapor. The gasoline vapor passes through the adsorbent to remove the gasoline component, and becomes clean air having a gasoline concentration lower than 1 vol%, and is discharged to the atmosphere via the exhaust valve 64a. The adsorption desorption tower n, 61 Regardless of the function of adsorption and desorption of gasoline vapor, the temperature medium supplied by the liquid circulation pump 8 is always used to cool to a fixed temperature. That is, the cooling system for the first condensation device 9 and the adsorption desorption column 丨i, ® 61 is always The operation control is performed in such a manner that the temperature of the system is set to 0 to 5 ° C. Next, the desorption treatment of the gasoline vapor will be described. In the case of desorbing the fly oil adsorbed by the adsorbent, The getter pump 13 draws in gas from the adsorption/desorption column 61, and desorbs the gasoline by the adsorbent. At this time, the desorbing valve 63b is opened in advance to close 63a. Although the adsorption tower is in the 〇1]y [pa In the atmospheric pressure state, the gasoline adsorbed by the adsorbent is desorbed by the pressure difference due to the pressure drop to the atmospheric pressure or lower during the desorption. The desorbed gasoline vapor is pressurized by the pressurizing pump 14, Supply 2118-8326-PF 31 1327164 Three-condensing device i 15. The pressure controller 19 maintains the pressure inside the third condensing device 于 at a high pressure of 0.3 MPa, and efficiently liquefies the gasoline vapor into the lamp. The gasoline vapor discharged from the pressure controller 19 is returned to the second condensation M 1G, and the gasoline component is again coagulated (4), and then returned to the adsorption solution, the column 11. During the repetition of this operation, the coagulation device 9, (7), and 15 are coagulated and recovered for the entire amount of gasoline. The desorption method using the pressure difference of the getter pump 13 is effective because it is not too south in efficiency. In the seventh embodiment, the portion of the clean gas discharged to the atmosphere is sent to the desorption column 61 via the gas flow rate adjustment method, and the first gas is used. In this case, the gas flow rate adjusting valve 6 is in a state in which the rolling body of the opening type to the gauge 1 can flow, and the gas flow rate adjusting valve "a is closed, and the gas does not flow. Further, in the seventh embodiment, Since the first-coagulation device 9 in the preceding stage sufficiently lowers the content in the gas, the moisture contained in the flushing gas has no adverse effect on the suction in the third adsorption desorption column. The oil supply to the storage tank is generally fixed for a fixed period of time. Therefore, the production of poetry, the occupation of friends, and the 'U gas are limited to the fixed time of the day _ / standing > In the present embodiment, since the adsorption operation and the desorption operation are simultaneously performed, and the adsorption operation and the desorption operation are performed in series, the first operation example in which the analysis time can be extended can be said to have a low operation rate because the adsorption operation is performed at the same time. The desorption operation can be stopped when the adsorption operation or the desorption operation is not performed, that is, the cooling can be stopped without recovering the gasoline vapor, and the energy used for cooling can be reduced, which can be said to be an energy-saving machine.

2118-8326-PF 32 1327164 From the above, it is possible to perform energy-saving and high-efficiency gasoline recovery by performing the operation while performing the adsorption operation and the desorption operation simultaneously. Next, the switching of the adsorption/desorption columns 11, 61 will be described. In the seventh embodiment, the case where the adsorption/desorption columns 11 and 61 are switched using a timer will be described. As described above, the gasoline vapor is adsorbed and removed by the first adsorption desorption column 丨i, and becomes a clean air having a gasoline concentration of less than 1 vol%, and is discharged to the atmosphere via the exhaust valve 64a. However, as the amount of gasoline vapor supplied to the first adsorption/desorption column 11 increases, the adsorption enthalpy of the first adsorption/desorption column 11 gradually decreases. This state continues, and when the gasoline concentration at the outlet of the first adsorption desorption column 1 is close to lv〇l%, it is necessary to switch the adsorption desorption columns U, 6ι. Since the gas station's oil supply to the gasoline storage tank 1 is regularly fixed for a fixed period of time, it is the simplest control to simply switch to a fixed time after starting the recovery. Therefore, the switching between the adsorption/desorption columns i i and 61 is effective when the three-way switching valve 3a has been switched or when the recovery device is operated as the starting time. Further, in the actual switching operation, the mode in which the suction valves 62a and 62b are not closed at the same time and the gasoline vapor is always flowing, and the switching is preferably performed. In other words, when the adsorption is performed by the first adsorption/desorption column 11 and the third adsorption/desorption column 61 is desorbed, the closed adsorption valve 62b, the desorption valve 63a, and the exhaust valve 64b are opened, and then Switching is preferably performed such that the suction valve 62a, the desorption valve 63b, and the exhaust valve 64a that are originally opened are in a closed state. Thereby, a safe gasoline recovery device can be provided, which does not supply the gasoline desorption tower 11, 61 gasoline vapor, nor does the oil supply speed to the gasoline storage tank 1 slow down, or the pressure in the gasoline storage tank i changes. high. Finally, the treatment of gaseous hydrocarbons in the seventh embodiment will be described, and the return 2118-8326-PF 33 1327164

The control method of the receiving device. When the recovery device is stopped, the intake pump 13 or the pressurized fruit juice is stopped, the adsorption valves 62a and 62b, the desorption valve core, 631), and the exhaust valve material are in a fully closed state, and the gas flow rate adjustment valves 65a and 65b are closed. Is off. When the three-way switching valve 3a is switched, an operation signal is received, for example, a switching signal of the three-way switching valve 3a is received, and the suction valve 62a desorbing valve 63b and the exhaust gas (four) are turned on. , ^ & storage tank 1 starts to supply oil, and gasoline vapor flow first - condensing farm 9, second condensing device ίο, and first adsorption desorption tower u. The suction spring 13 and the pressure pump 14 are operated simultaneously with the start of the adsorption operation. By the operation of the suction pump 13, and the pressure of the third adsorption solution 61 is lowered to a predetermined pressure, the gas flow adjustment valve (10) starts to open to control the gas flow adjustment valve by a predetermined flow rate to the third adsorption desorption column. The opening of 65b. "According to the above method, after the fuel supply is fixed for a fixed period of time, the adsorption desorption: 61 is switched. When the switching signal is received by the timer or the like, the closed adsorption valve 62b, the desorption valve 63a, and the row are closed as described above. The gas valve _ is in an open state, and the gas flow rate adjustment valve 65b is in a closed state. Then, the adsorption bleeder, the desorption reading 63b, and the exhaust valve 64a are turned on, and the third adsorption/desorption column 61 becomes an adsorption operation, and the first - The money desorption column U becomes a desorption operation. By the operation of the getter pump 13, and the pressure of the third adsorption desorption column 61 is reduced to the same pressure, the gas flow regulating valve starts to open, and flows to the third adsorption desorption column at a predetermined flow rate. In the manner of 61, the opening degree of the gas flow regulating valve 65b is controlled. According to this step, the switching operation is repeated, and when the fuel supply of the gasoline storage tank 1 is stopped, the three-way reversing (five) 3 "knife change, after receiving the stop signal" sucks The air pump 13 or the pressure pump 14 is stopped, the gas flow rate adjustment valve 65b is turned off, and the adsorption valve 62 & the desorption valve (four), and the row

2118-8326-PF 34 The air valve 64a is turned off. As described above, the treatment and recovery device for gaseous hydrocarbons in the seventh embodiment is a combination of two condensation devices 9 and 1 in the temperature zone and the adsorption/desorption columns 11 and 61. 〇 1% of gasoline vapor is a treatment and recovery device for gaseous hydrocarbons with little environmental load. In addition, since only up to 1 vol% of gasoline vapor is discharged, 39% of the 4 ν ν% of gasoline vapor can be recovered, and the recovery efficiency is 97 5%, which is a highly efficient recovery device. Further, since the adsorption operation is performed after the coagulation operation is performed, the adsorption/desorption columns 11 and 61 can be made small, and the entire device can be miniaturized. In addition, since the adsorption operation and the desorption operation are simultaneously performed, the unhelpful operation can be reduced, and the running cost can be reduced. (Embodiment 8) FIG. 13 is a view showing an overall configuration of a flow of a gaseous hydrocarbon processing and recovery apparatus according to an eighth embodiment of the present invention. The difference between the eighth embodiment and the seventh embodiment is that the flow of the gas treatment at the time of regeneration of the first adsorption/desorption column 11 is different. Further, in the configuration of the eighth embodiment, as shown in Fig. 13, the pressure pump 14, the third condensing device 15, and the pressure controller 19 are not included in the drawing. In the seventh embodiment, the gasoline vapor desorbed by the air suction pump 13 by the third adsorption/desorption column 61 is pressurized by the pressure pump 14, and then supplied to the third condensation device 15. The gasoline vapor passing through the third condensing device 15 is discharged to the atmosphere through the second condensing device 10 and the first adsorption/desorption column 11. However, in the eighth embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption column u is supplied to the first condensation device 9. The first coagulation device 9 merges with the gasoline vapor discharged from the gasoline storage tank 1, and is discharged to the atmosphere through the first coagulation device 2118-8326-PF 35 1327164 9 and the first adsorption desorption column U. This simplifies system construction and reduces the cost of the unit. • From the above, by removing the pressurizing pump 14, the third condensing device 15, and the pressure (four) stomach 19, there is a low-cost and energy-saving returning device. [Embodiment 9] Fig. 14 is a view showing an overall configuration of a flow of a gaseous hydrocarbon processing and recovery apparatus according to a ninth embodiment of the present invention. The difference between the ninth embodiment and the seventh embodiment is that the flow of the gas treatment at the time of regeneration of the first adsorption/desorption column 11 is different. Further, in the configuration of the seventh embodiment, as shown in Fig. 12, the inside of the third condensing device 15 is cooled to 〇5 by the temperature medium. In the ninth embodiment, as shown in Fig. 14, the fourth condensing device 51 which is directly cooled by the refrigerator 5 by the refrigerant is formed. In the seventh embodiment, the sputum oil vapor desorbed by the air suction pump 13 by the first adsorption/desorption column u is pressurized by the pressurizing pump 14, and then supplied to the third condensing device 15. The gasoline vapor passing through the third condensing device 15 is discharged to the atmosphere through the second condensing device 10 and the first adsorption/desorption column U. However, in the ninth embodiment, the gasoline vapor desorbed by the air suction pump 13 by the first adsorption/desorption tower is pressurized by the pressure pump 14, and then supplied to the fourth condensation device 51. The inside of the fourth condensing device 51 is directly cooled by the refrigerant cooled by the refrigerator 5 to become about 30 °C. The gasoline vapor concentration becomes about lv 〇 1% under the conditions of a pressure of 〇 3 MPa and a cooling temperature of 30 ° C, and is supplied to the first adsorption/desorption column 11 . Thereby, the amount of gasoline vapor adsorbed and removed by the first adsorption desorption column 丨i can be reduced, and the switching time of the adsorption desorption columns 11, 61 can be increased, and the long life of 2118-8326-PF 36 1327164 can be extended. In addition, m recognizes that it can achieve a safer operation because it can reduce the number of switching times. From the above, the fourth condensing device 5 1, a a including the third condensing device 15 is provided with a recovery device which can provide low cost and high reliability. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a view showing an overall configuration of a process for treating and recovering a gaseous hydrocarbon according to a first embodiment of the present invention.

Fig. 2 is a characteristic diagram showing the relationship between the cooling temperature and the amount of silicone filling. Fig. 3 is a characteristic diagram for explaining a method of controlling the amount of gas for flushing. Fig. 4 is a characteristic diagram showing the relationship between the flow rate of the treatment gas and the recovery rate. Fig. 5 is a characteristic diagram showing the relationship between the internal pressure and the amount of silicone filling. Fig. 6 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the first embodiment of the present invention. Fig. 7 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the second embodiment of the present invention. Fig. 8 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the third embodiment of the present invention. Fig. 9 is a view showing the overall configuration of a flow of a gaseous carbon argon treatment and recovery apparatus according to a fourth embodiment of the present invention. Fig. 1 is a view showing the overall structure of a process for treating and recovering gaseous hydrocarbons 2118-8326-PF 37 LU^f according to the fifth embodiment of the present invention. Fig. U is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the sixth embodiment of the present invention. Fig. 12 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the seventh embodiment of the present invention. Fig. 13 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the eighth embodiment of the present invention. Fig. 14 is a view showing the overall configuration of the flow of the gaseous hydrocarbon processing and recovery apparatus according to the ninth embodiment of the present invention. [Main component symbol description] 1 Gasoline storage tank 2 Oil supply pipe 3 Two-way switching valve 4 Pressure regulating valve 5 Freezer 6 Heat exchanger 7 Temperature medium tank 8 Liquid circulation system · 9 First condensation device 10 Second condensation device 11 First adsorption desorption tower 12 Two-way valve 13 Suction pump 14 Pressurized fruit 15 Third condensation device 16 Second adsorption desorption tower 17 Flow adjustment valve 18 Gasoline piping 19 Pressure controller 21 Valve 31 Pressure buffer container 32 Pressure measurement 41 gas storage container 42 main flow controller 43 shut-off valve 51 fourth coagulation device 61 third adsorption desorption column 62 adsorption valve 63 65 desorption valve gas flow adjustment valve 64 exhaust valve 2118-8326-PF 38

Claims (1)

1327164 No. 095134421 Chinese Patent Application Amendment Revision Date: 98.12.11 X. Patent application scope: 1. A gas-like hydrocarbon treatment, IA recovery device, which recovers gasoline vapor leaking during oil supply, characterized by: First condensation device, which removes moisture contained in gasoline vapor And a second condensing device for removing gasoline vapor from the gasoline, disposed on the downstream side of the gas in the subsequent stage of the first condensing device; the first adsorbing and desorbing device disposed on the downstream side of the gas in the subsequent stage of the second condensing device; the getter pump The gasoline vapor is taken out by the first adsorption desorption device; the gasoline pump pressurizes the gasoline vapor taken out by the air suction pump; the third condensation device removes the pressurized gasoline vapor; and the second adsorption desorption device recovers The gasoline vapor that cannot be recovered by the third condensing device. 2. For the treatment and recovery of gaseous hydrocarbons in the first application of the patent scope, in which the fin tube heat exchanger is disposed inside the adsorption desorption device, and the pore size of the adsorbent is 4 to 1 〇〇. A monomer of a silicone or synthetic zeolite or a mixture thereof is placed between the fins of the tab tube heat exchanger. 3. The cooling temperature phase of the gas-like hydrocarbon treatment, recovery unit/, medium-made junction device and second condensation device in the scope of patent application No. 1 -30〇C. 2118-8326-PF1 4: The treatment and recovery of gaseous hydrocarbons according to item 1 of the patent application range is from 0 ° C to about 5. (:, 39 1327164 5. For the treatment and recovery of gaseous hydrocarbons in the first paragraph of the patent application scope, 'Use: Cooling path' uses a temperature medium controlled by a cold or a cooling device. Cooling; and cooling path, using a temperature medium filled with cold or cooling through cooling to control the temperature of the coagulation device and the adsorption desorption device. 6. A method for treating and recovering gaseous hydrocarbons for treatment The gasoline vapor leaking when the π oil is supplied, the gas hydrocarbon treatment and recovery device comprises: a first condensing device for removing moisture and gasoline vapor; and a second condensing device for removing gasoline vapor, and placing the first condensing device After the device, (4) the downstream side of the gas, and the adsorption and desorption device of the gasoline vapor, disposed on the downstream side of the gas in the subsequent stage of the second condensing device, wherein the adsorption desorption device has at least one adsorption tower higher than (TC) Space, ancient recognition ° ^ back to a 3 (TC space, and the filling of the adsorbent in the order of processing gasoline vapor. I, Shenyue patent $ & surrounding the sixth item The treatment and recovery of gaseous hydrocarbons, wherein the adsorption desorption ‘ desorption time is set to be greater than 1 hour. 2118-8326-PF1 40