CN114011208A - Gasoline vapor recovery unit - Google Patents
Gasoline vapor recovery unit Download PDFInfo
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- CN114011208A CN114011208A CN202111231984.0A CN202111231984A CN114011208A CN 114011208 A CN114011208 A CN 114011208A CN 202111231984 A CN202111231984 A CN 202111231984A CN 114011208 A CN114011208 A CN 114011208A
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- 238000011084 recovery Methods 0.000 title claims abstract description 41
- 239000002250 absorbent Substances 0.000 claims abstract description 81
- 230000002745 absorbent Effects 0.000 claims abstract description 81
- 238000001179 sorption measurement Methods 0.000 claims abstract description 77
- 239000003463 adsorbent Substances 0.000 claims abstract description 52
- 238000010521 absorption reaction Methods 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 238000012806 monitoring device Methods 0.000 claims abstract description 15
- 230000008929 regeneration Effects 0.000 claims abstract description 13
- 238000011069 regeneration method Methods 0.000 claims abstract description 13
- 238000004891 communication Methods 0.000 claims abstract description 8
- 238000001514 detection method Methods 0.000 claims abstract description 8
- 238000000926 separation method Methods 0.000 claims abstract description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 19
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 239000000741 silica gel Substances 0.000 claims description 12
- 229910002027 silica gel Inorganic materials 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 238000012544 monitoring process Methods 0.000 claims description 3
- 230000008676 import Effects 0.000 claims 1
- 239000003921 oil Substances 0.000 description 56
- 238000000034 method Methods 0.000 description 8
- 230000007613 environmental effect Effects 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000006096 absorbing agent Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
Abstract
The utility model provides a gasoline oil gas recovery device, which comprises an absorption tower, a coalescer, an adsorption device, a vacuum pump, a temperature monitoring device, an emission concentration detection device and a temperature adjusting device, wherein the absorption tower is used for leading an absorbent accessed through an absorbent inlet and a gasoline oil gas accessed through a gasoline oil gas inlet to be in countercurrent contact in the vertical direction so as to lead the absorbent to absorb the gasoline in the gasoline oil gas; the coalescer is used for receiving the gasoline oil gas treated by the absorbent of the absorption tower and enabling the coalescer to carry out further gas-liquid separation; the adsorption device is provided with an adsorbent used for adsorbing the gasoline from the gas which moves from bottom to top and carries the residual gasoline; the vacuum pump is used for carrying out vacuum regeneration on the adsorbent; the temperature adjusting device is in communication connection with the emission concentration detecting device and the temperature monitoring device, and adjusts the temperature of the external absorbent. The absorption tower, the coalescer and the adsorption device are used for carrying out the gasoline oil gas treatment for three times, so that the content of the discharged gas containing gasoline is reduced.
Description
Technical Field
The disclosure relates to the field of oil gas recovery, and more particularly relates to a gasoline oil gas recovery device.
Background
In the loading process of oil products, oil gas generated by volatilization of gasoline products is dissipated to the top of the tank car and is exhausted to the atmosphere, the volatilized oil gas has the characteristics of flammability and explosiveness, the concentration is high, and the volatilized oil gas and air form explosive gas which is distributed in the upper space of the tank car and around the loading exhaust port of the tank car, so that the volatile oil gas is extremely easy to explode when meeting open fire, and the safety production is influenced. For this reason, recovery of the volatilized oil gas is required.
Although an oil gas recovery device is arranged on the volatilized oil gas at present, the emission concentration of the discharged gas containing gasoline after being treated by the oil gas recovery device is required to be lower and lower due to the increasingly strict environmental protection requirement. Therefore, it is necessary to further reduce the emission concentration of the gasoline-containing gas discharged after the recovery treatment, which is advantageous for environmental protection.
Disclosure of Invention
In view of the problems in the background art, it is an object of the present disclosure to provide a gasoline vapor recovery device that can reduce the emission concentration of a gasoline-containing gas discharged after being treated by the gasoline vapor recovery device.
Therefore, in some embodiments, the gasoline oil gas recovery device comprises an absorption tower, a coalescer, an adsorption device, a vacuum pump, a temperature monitoring device, an emission concentration detection device and a temperature regulation device, wherein the absorption tower is provided with an absorbent inlet, a gasoline oil gas inlet and a discharge port, the absorbent inlet is positioned above the gasoline oil gas inlet, the discharge port is positioned above the absorbent inlet, the absorbent inlet is used for connecting an external absorbent, the gasoline oil gas inlet is used for connecting gasoline oil gas of an external gasoline storage tank, the absorption tower is used for enabling the absorbent connected through the absorbent inlet and the gasoline oil gas connected through the gasoline oil gas inlet to be in countercurrent contact in the vertical direction, so that the absorbent absorbs the gasoline in the gasoline oil gas, the absorbent absorbing the gasoline becomes rich liquid and falls and is collected at the lower part of the absorption tower, and the discharge port is used for discharging the gasoline oil gas treated by the absorbent; the coalescer is provided with a first inlet and a first outlet, the first outlet is higher than the first inlet, the first inlet is communicated with the discharge port of the absorption tower and is used for receiving gasoline oil gas treated by the absorbent of the absorption tower and further separating gas and liquid in the coalescer, separated gasoline oil drops are collected at the lower part of the coalescer, and the separated gas carrying residual gasoline is discharged through the first outlet; the adsorption device is provided with an inlet, a discharge outlet and an adsorbent, the inlet is lower than the discharge outlet, the inlet of the adsorption device is communicated with the first outlet of the coalescer in a controlled mode and is used for receiving the gas carrying the residual gasoline from the coalescer, the adsorbent is arranged between the inlet and the discharge outlet in the vertical direction and is used for adsorbing the gasoline of the gas carrying the residual gasoline moving from bottom to top, and the discharge outlet is used for discharging the gas containing the gasoline passing through the adsorbent; the vacuum pump is controlled to be communicated with the adsorption device and is used for carrying out vacuum regeneration on the adsorbent of the adsorption device for adsorbing gasoline; the temperature monitoring device is used for monitoring the ambient temperature, the temperature of the external absorbent and the temperature of the external gasoline oil gas; the emission concentration detection device is used for detecting the concentration of the gas containing gasoline discharged from the discharge port of the adsorption device; the temperature adjusting device is in communication connection with the emission concentration detecting device and the temperature monitoring device, and the temperature adjusting device adjusts the temperature of the external absorbent based on the environment temperature monitored by the temperature monitoring device, the temperature of the external absorbent, the temperature of the external gasoline oil gas and the concentration of the gasoline-containing gas discharged from the discharge port of the adsorption device monitored by the emission concentration detecting device.
In some embodiments, the absorbent is gasoline.
In some embodiments, the absorption tower further comprises a rich liquid outlet for communicating with an external gasoline storage tank.
In some embodiments, the coalescer further has a second outlet disposed in a lower portion of the coalescer for communicating with an external gasoline storage tank.
In some embodiments, the adsorption devices are two and arranged in parallel, wherein one adsorption device is used for operation, and the other adsorption device is used as the one adsorption device to complete adsorption and is operated during regeneration, so that the two adsorption devices are alternately operated.
In some embodiments, the adsorbents of the adsorption device include multiple adsorbents that differ in their operating life under adsorption conditions by the type of adsorbent and the operating life being arranged from bottom to top, with the longest operating life adsorbent being placed closest to the inlet side, followed by the next longest operating life adsorbent, and so on.
In some embodiments, the adsorbent of the adsorption device comprises silica gel and activated carbon, the silica gel being proximate the inlet relative to the activated carbon, and the activated carbon being proximate the outlet relative to the silica gel.
In some embodiments, the vacuum pump is a dry vacuum pump.
In some embodiments, the vacuum pump is also in communication with a gasoline vapor inlet of the absorber to supply vacuum regeneration recovered gasoline from the adsorbent to the absorber.
In some embodiments, the temperature regulating device controls the temperature of the external absorbent to be between 3 ℃ and 5 ℃.
The beneficial effects of this disclosure are as follows: in the gasoline oil gas recovery device according to the disclosure, the absorption tower, the coalescer and the adsorption device are used for carrying out gasoline oil gas treatment for three times, so that the content of gasoline-containing gas discharged from the discharge port of the adsorption device is reduced, and further, increasingly strict environmental protection requirements are met.
Drawings
Fig. 1 shows a layout of a gasoline vapor recovery device according to the present disclosure.
Wherein the reference numerals are as follows:
100 gasoline vapor recovery unit 22 first outlet
D second outlet in up-down direction 23
1 absorption tower 3 adsorption device
11 absorbent inlet 31 inlet
12 gasoline oil gas inlet 32 discharge port
13 exhaust port 4 vacuum pump
14 rich liquid outlet 5 temperature monitoring device
2 coalescer 6 discharge concentration detection device
21 first inlet 7 temperature regulating device
Detailed Description
The accompanying drawings illustrate embodiments of the present disclosure and it is to be understood that the disclosed embodiments are merely examples of the disclosure, which can be embodied in various forms, and therefore, specific details disclosed herein are not to be interpreted as limiting, but merely as a basis for the claims and as a representative basis for teaching one skilled in the art to variously employ the present disclosure.
Referring to fig. 1, a gasoline vapor recovery device 100 includes an absorption tower 1, a coalescer 2, an adsorption device 3, a vacuum pump 4, a temperature monitoring device 5, an emission concentration detection device 6, and a temperature adjustment device 7.
The absorption tower 1 is provided with an absorbent inlet 11, a gasoline oil gas inlet 12 and a discharge port 13, the absorbent inlet 11 is positioned above the gasoline oil gas inlet 12, the discharge port 13 is positioned above the absorbent inlet 11, the absorbent inlet 11 is used for being connected with an external absorbent, the gasoline oil gas inlet 12 is used for being connected with the gasoline oil gas of an external gasoline storage tank, the absorption tower 1 is used for enabling the absorbent connected through the absorbent inlet 11 and the gasoline oil gas connected through the gasoline oil gas inlet 12 to be in countercurrent contact in the vertical direction D so that the absorbent absorbs the gasoline in the gasoline oil gas, the absorbent absorbing the gasoline falls into rich liquid and is collected at the lower part of the absorption tower 1, and the discharge port 13 is used for discharging the gasoline oil gas treated by the absorbent;
the coalescer 2 is provided with a first inlet 21 and a first outlet 22, the first outlet 22 is higher than the first inlet 21, the first inlet 21 is communicated with the discharge port 13 of the absorption tower 1 and is used for receiving the gasoline oil gas treated by the absorbent of the absorption tower 1 and further carrying out gas-liquid separation on the coalescer 2, separated gasoline oil drops are collected at the lower part of the coalescer 2, and the separated gas carrying residual gasoline is discharged through the first outlet 22;
the adsorption device 3 has an inlet 31, a discharge port 32, and an adsorbent, the inlet 31 is lower than the discharge port 32, the inlet 31 of the adsorption device 3 is controlled to communicate with the first outlet 22 of the coalescer 2 and is used for receiving the residual gasoline carrying gas from the coalescer 2, the adsorbent is disposed between the inlet 31 and the discharge port 32 in the up-down direction D and is used for adsorbing gasoline from the residual gasoline carrying gas moving up and down, and the discharge port 32 is used for discharging the gasoline containing gas passing through the adsorbent.
The vacuum pump 4 is in controlled communication with the adsorption device 3 and is used for vacuum regeneration of the adsorbent of the adsorption device 3, which adsorbs gasoline.
The temperature monitoring device 5 is used for monitoring the ambient temperature, the temperature of the external absorbent and the temperature of the external gasoline oil gas.
The emission concentration detection means 6 is for detecting the concentration of the gas containing gasoline discharged from the discharge port 32 of the adsorption device 3.
The temperature adjusting device 7 is in communication connection with the emission concentration detecting device 6 and the temperature monitoring device 5, and the temperature adjusting device 7 adjusts the temperature of the external absorbent based on the ambient temperature monitored by the temperature monitoring device 5, the temperature of the external absorbent, the temperature of the external gasoline vapor, and the concentration of the gasoline-containing gas discharged from the discharge port 32 of the adsorption device 3 monitored by the emission concentration detecting device 6.
In the gasoline vapor recovery device 100 according to the present disclosure, the absorption tower 1, the coalescer 2, and the adsorption device 3 are used to perform gasoline vapor treatment three times, so that the content of the gas containing gasoline discharged from the discharge port 32 of the adsorption device 3 is reduced, thereby satisfying further stricter and stricter (i.e., lower and lower discharge concentration) environmental requirements.
The external gasoline storage tank accessed by the gasoline gas inlet 12 can come from a tank truck or an oil depot.
In one example, the external absorbent that the absorbent inlet 11 taps into is gasoline. The gasoline is used as an absorbent, so that the countercurrent absorption of gasoline oil gas is more effective, the gasoline recovered after treatment by the absorption tower 1 and the coalescer 2 can be directly returned to an external gasoline storage tank, and the gasoline recovered after treatment by the vacuum pump 4 of the dry vacuum pump can be directly returned to the absorption tower 1, so that the separation and recovery operation is not required to be carried out by adopting a non-gasoline absorbent, the process is simplified, the efficiency is improved, and the quantity of the gasoline delivered to the outside of the external gasoline storage tank is increased.
As shown in fig. 1, the absorption tower 1 further includes a rich liquid outlet 14, and the rich liquid outlet 14 is used for communicating with an external gasoline storage tank. The rich liquid collected at the lower part of the absorption tower 1 is pure gasoline under the condition that the external absorbent is gasoline, and the gasoline is directly recycled to the external gasoline storage tank through the rich liquid outlet 14, so that the quantity of the gasoline which is externally delivered by the external gasoline storage tank is increased.
Similarly, with reference to fig. 1, the coalescer 2 also has a second outlet 23, the second outlet 23 being disposed in the lower portion of the coalescer 2, the second outlet 23 being for communication with an external gasoline storage tank. In the coalescer 2, the gasoline droplets collected in the lower part of the coalescer 2 are pure gasoline in the case that the absorbent on the outside is gasoline, and the gasoline is directly recycled to the external gasoline storage tank through the second outlet 23, thereby increasing the amount of gasoline to be delivered to the external gasoline storage tank.
In the example shown in fig. 1, the adsorption apparatuses 3 are two and arranged in parallel, wherein one adsorption apparatus 3 is used for operation, and the other adsorption apparatus 3 performs adsorption as the one adsorption apparatus 3 and operates at the time of regeneration, so that the two adsorption apparatuses 3 operate alternately. Because the adsorbent of the adsorption device 3 is loaded in the adsorption device 3, which is different from the continuous connection of the adsorbent of the absorption tower 1 from the outside, the adsorbent of the adsorption device 3 can be replaced only after the adsorption device 3 is stopped, and the arrangement of two adsorption devices 3 improves the continuous working time of the gasoline oil-gas recovery device 100, and avoids the work pause of the gasoline oil-gas recovery device 100 caused by the stop of the gasoline oil-gas recovery device 100 because the adsorbent of the adsorption device 3 is required to be regenerated after the service life of the adsorbent is finished by only one adsorption device 3. Of course, the number of the adsorption devices 3 may be more than two.
Since the adsorbent is treated with different loads from the inlet 31 to the discharge 32 during the operation of the adsorption apparatus 3, the adsorbent at the inlet 31 is saturated first compared with the adsorbent at the discharge 32, and the whole shutdown of the adsorption apparatus 3 is usually performed to replace the adsorbent based on the saturation of the adsorbent at the inlet 31, so as to overcome the difference caused by the saturation of the adsorbent from the inlet 31 to the discharge 32 of the adsorption apparatus 3 along with the continuation of the adsorption process, the adsorbent of the adsorption apparatus 3 includes a plurality of adsorbents, the plurality of adsorbents have different working lives under the adsorption condition, the plurality of adsorbents are arranged from bottom to top according to the kinds and working lives of the adsorbents, the kind of the adsorbent having the longest working life is arranged at the side closest to the inlet 31, the kind of the adsorbent having the second longest working life is arranged, and so on. This allows the various adsorbents to reach saturation as much as possible at the same time as the adsorption process continues. Thus, not only the various adsorbents fully and completely function, but also the adsorption effect is in a constant state (i.e., from the state of being newly loaded to the state of being completely saturated) during the whole operation process before the regeneration of the adsorption device 3, which is beneficial to the consistency of the concentration of the gas containing gasoline discharged from the discharge port 32 of the adsorption device 3 during the long-time operation of the gasoline vapor recovery device 100, thereby improving the stability of the discharge quality during the long-time operation process of the vapor recovery device 100.
In one example, the adsorbent of the adsorption device 3 includes silica gel and activated carbon, the silica gel being adjacent to the inlet 31 relative to the activated carbon, and the activated carbon being adjacent to the outlet 32 relative to the silica gel.
In one example, the vacuum pump 4 is a dry vacuum pump. Compared with the method using oil, water or other polymer medium as the working medium of the pump, the dry vacuum pump only uses air and does not use oil, water or other polymer medium, so that the gasoline recovered when the adsorbent of the adsorption device 3 is regenerated by the dry vacuum pump through vacuum pumping does not contain impurities carried by the medium of the vacuum pump 4. When the absorbent of the absorption tower 1 adopts gasoline, the gasoline recovered by the vacuum regeneration of the dry vacuum pump 4 is gas-carried gasoline, which is exactly consistent in composition and shape with the generated gasoline of the external gasoline storage, so further, in the example shown in the figure, the vacuum pump 4 is also communicated with the gasoline and gasoline inlet 12 of the absorption tower 1 to supply the gasoline recovered by the vacuum regeneration from the absorbent to the absorption tower 1. Thus, not only is the need to separately treat the recovered gasoline upon vacuum regeneration by the vacuum pump 4 avoided, but also the recovery of gasoline and the reduction in the concentration of the final gasoline-containing gas emissions are enhanced. In the example shown in the figure, the temperature regulation device 7 is provided directly on the line of the absorbent supply to the absorbent inlet 11 of the absorption column 1. The temperature adjusting device 7 adjusts the temperature of the absorbent by means of a water jacket, for example. In other embodiments, the temperature adjustment device 7 may be provided adjacent to the line of the absorbent inlet 11 of the absorbent supply to the absorption column 1.
In one example, the temperature regulating device 7 controls the temperature of the external absorbent to 3 ℃ to 5 ℃. The temperature is too low (namely lower than 3 ℃), so that the mobility of the gasoline is poor when the gasoline is used as an absorbent, the gasoline is not beneficial to the absorption of the gasoline in the gasoline oil gas after the gasoline used as the absorbent enters the absorption tower 1 and is in countercurrent contact with the absorbent accessed through the absorbent inlet 11 and the gasoline oil gas accessed through the gasoline oil gas inlet 12 in the vertical direction D, and meanwhile, the requirements of equipment, media and the like for adjusting the absorbent to be at lower temperature of the temperature regulator device 7 are increased (namely, the lower the temperature is, the more strict the requirements are); the temperature is too high (namely higher than 5 ℃), the gasoline as the absorbent volatilizes, which increases the amount of gasoline oil gas on the basis of the gasoline oil gas itself accessed through the gasoline oil gas inlet 12, if the gasoline as the absorbent volatilizes, the volatilized gasoline oil gas from the absorbent is directly discharged to the coalescer 2 through the discharge port 13 positioned above the absorbent inlet 11 because the aforementioned countercurrent adsorption cannot be carried out, so that the adsorption effect of the absorption tower 1 is reduced, and the discharge concentration of the gasoline-containing gas discharged through the discharge port 32 may be increased in the case of using the same coalescer 2 and adsorption device 3.
Finally, test examples are given.
Example 1
The whole structure and the path arrangement of the figure 1 are adopted, the geometric similarity miniaturization test with the same proportion is carried out in a laboratory, and the running condition of the whole gasoline oil-gas recovery device is simulated through HYSYS. The absorbent adopts gasoline, the absorbent of the absorption device 3 adopts silica gel and active carbon, the silica gel is close to the inlet 31 relative to the active carbon, the active carbon is close to the discharge outlet 32 relative to the silica gel, the vacuum pump 4 adopts a dry vacuum pump, the temperature of the gasoline used as the absorbent is controlled to be 3 ℃, and the temperature of the gasoline oil gas connected into the gasoline oil gas inlet 12 is 30 ℃ in summer.
The oil gas recovery efficiency reaches 98%, and the emission concentration is 8-13 g/m3Left and right.
Wherein, GB 20950 and 2007 appendix B of the atmospheric pollutant emission standard of oil-gas recovery efficiency in oil storage.
Example 2
The same procedure as in example 1 was repeated, except that the temperature of the gasoline as an absorbent was controlled to 5 ℃.
The oil gas recovery efficiency reaches 97%, and the emission concentration is 12-15 g/m3Left and right.
Comparative example 1
Only the coalescer of fig. 1 is removed.
The oil gas recovery efficiency reaches 95, and the emission concentration is 20-25 g/m3Left and right.
Comparative example 2
The temperature of the gasoline used as the absorbent alone was controlled at 2 c, as in example 1.
The oil gas recovery efficiency reaches 96.5, and the emission concentration is 10-14g/m3Left and right.
Comparative example 3
The temperature of the gasoline used as the absorbent alone was controlled at 6 c, as in example 1.
The oil gas recovery efficiency reaches 96.5, and the emission concentration is 14-17g/m3Left and right.
The above detailed description is used to describe a number of exemplary embodiments, but is not intended to limit the combinations explicitly disclosed herein. Thus, unless otherwise specified, various features disclosed herein can be combined together to form a number of additional combinations that are not shown for the sake of brevity.
Claims (10)
1. A gasoline oil gas recovery device (100) is characterized by comprising an absorption tower (1), a coalescer (2), an adsorption device (3), a vacuum pump (4), a temperature monitoring device (5), an emission concentration detection device (6) and a temperature adjusting device (7),
the absorption tower (1) is provided with an absorbent inlet (11), a gasoline oil gas inlet (12) and a discharge port (13), the absorbent inlet (11) is positioned above the gasoline oil gas inlet (12), the discharge port (13) is positioned above the absorbent inlet (11), the absorbent inlet (11) is used for being connected with an external absorbent, the gasoline oil gas inlet (12) is used for being connected with gasoline oil gas of an external gasoline storage tank, the absorption tower (1) is used for enabling the absorbent connected through the absorbent inlet (11) and the gasoline oil gas connected through the gasoline oil gas inlet (12) to be in countercurrent contact in the vertical direction (D) so that the absorbent absorbs gasoline in the gasoline oil gas, the absorbent for absorbing the gasoline becomes rich liquid and falls and is collected at the lower part of the absorption tower (1), and the discharge port (13) is used for discharging the gasoline oil gas treated by the absorbent;
the coalescer (2) is provided with a first inlet (21) and a first outlet (22), the first outlet (22) is higher than the first inlet (21), the first inlet (21) is communicated with the discharge port (13) of the absorption tower (1) and is used for receiving gasoline oil gas treated by the absorbent of the absorption tower (1) and enabling the coalescer (2) to carry out further gas-liquid separation, separated gasoline oil drops are collected at the lower part of the coalescer (2), and separated gas carrying residual gasoline is discharged through the first outlet (22);
the adsorption device (3) is provided with an inlet (31), a discharge outlet (32) and an adsorbent, the inlet (31) is lower than the discharge outlet (32), the inlet (31) of the adsorption device (3) is communicated with the first outlet (22) of the coalescer (2) in a controlled manner and is used for receiving residual gasoline-carrying gas from the coalescer (2), the adsorbent is arranged between the inlet (31) and the discharge outlet (32) along the up-and-down direction (D) and is used for carrying out gasoline adsorption on the residual gasoline-carrying gas moving from bottom to top, and the discharge outlet (32) is used for discharging the gasoline-containing gas passing through the adsorbent;
the vacuum pump (4) is controlled to be communicated with the adsorption device (3) and is used for performing vacuum regeneration on the adsorbent for adsorbing gasoline of the adsorption device (3);
the temperature monitoring device (5) is used for monitoring the ambient temperature, the temperature of the external absorbent and the temperature of the external gasoline oil gas;
the emission concentration detection device (6) is used for detecting the concentration of the gas containing gasoline discharged from the discharge port (32) of the adsorption device (3);
the temperature adjusting device (7) is in communication connection with the emission concentration detecting device (6) and the temperature monitoring device (5), and the temperature adjusting device (7) adjusts the temperature of the external absorbent based on the ambient temperature monitored by the temperature monitoring device (5), the temperature of the external absorbent, the temperature of external gasoline oil gas and the concentration of the gasoline-containing gas discharged from the discharge port (32) of the adsorption device (3) monitored by the emission concentration detecting device (6).
2. The gasoline vapor recovery device (100) of claim 1, wherein the absorbent is gasoline.
3. The gasoline vapor recovery device (100) of claim 2, wherein the absorption tower (1) further comprises a rich liquid outlet (14), and the rich liquid outlet (14) is used for being communicated with an external gasoline storage tank.
4. The gasoline vapor recovery device (100) of claim 2, wherein the coalescer (2) further has a second outlet (23), the second outlet (23) being disposed at a lower portion of the coalescer (2), the second outlet (23) being for communication with an external gasoline storage tank.
5. The gasoline vapor recovery device (100) of claim 1,
the adsorption devices (3) are arranged in parallel, wherein one adsorption device (3) is used for working, and the other adsorption device (3) is used as the adsorption device (3) to complete adsorption and works during regeneration, so that the two adsorption devices (3) work alternately.
6. The gasoline vapor recovery device (100) of claim 2,
the adsorbent of adsorption equipment (3) includes multiple adsorbent, and the working life of multiple adsorbent under the adsorption condition is different, multiple adsorbent is arranged from bottom to top according to the kind and the working life of adsorbent, and the kind of the adsorbent that the working life is the longest is placed in and is closest to import (31) side, and secondly is the kind of the adsorbent that the working life is the second longest, and so on.
7. The gasoline vapor recovery device (100) of claim 6, characterized in that the adsorbent of the adsorption device (3) comprises silica gel and activated carbon, the silica gel being adjacent to the inlet (31) and the activated carbon being adjacent to the discharge (32) relative to the silica gel.
8. The gasoline vapor recovery device (100) of claim 2, wherein the vacuum pump (4) is a dry vacuum pump.
9. The gasoline vapor recovery device (100) of claim 8, characterized in that the vacuum pump (4) is further communicated with the gasoline vapor inlet (12) of the absorption tower (1) to supply the vacuum regeneration recovered gasoline from the adsorbent to the absorption tower (1).
10. The gasoline vapor recovery device (100) of claim 2, wherein the temperature regulating device (7) controls the temperature of the external absorbent to 3 ℃ to 5 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111231984.0A CN114011208B (en) | 2021-10-22 | 2021-10-22 | Gasoline and oil gas recovery device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111231984.0A CN114011208B (en) | 2021-10-22 | 2021-10-22 | Gasoline and oil gas recovery device |
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| CN114011208A true CN114011208A (en) | 2022-02-08 |
| CN114011208B CN114011208B (en) | 2024-04-09 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115678589A (en) * | 2022-11-18 | 2023-02-03 | 青岛飞普思环保科技有限公司 | Oil absorption process for oil gas recovery in light oil loading process |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201505500U (en) * | 2009-03-23 | 2010-06-16 | 江苏工业学院 | Oil and gas recovery device by absorption and adsorption integration technology |
| CN102441313A (en) * | 2010-10-12 | 2012-05-09 | 中国石油化工股份有限公司 | Oil gas recovery method |
| CN104815524A (en) * | 2015-04-09 | 2015-08-05 | 北京信诺海博石化科技发展有限公司 | Recovery technology for chemicals oil gas or mixed oil gas of chemicals and oil product |
| CN207749076U (en) * | 2017-12-06 | 2018-08-21 | 北京华清微拓节能技术股份公司 | A kind of refinery product's upgrading synergy and hydrogen recovery system |
| CN111569613A (en) * | 2020-05-26 | 2020-08-25 | 唐山三友硅业有限责任公司 | Device and method for eluting trace siloxane in organic silicon hydrolyzed HCl gas |
| CN113136246A (en) * | 2020-01-17 | 2021-07-20 | 北京航天石化技术装备工程有限公司 | High-temperature garbage dry distillation oil-gas separation system and method |
-
2021
- 2021-10-22 CN CN202111231984.0A patent/CN114011208B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201505500U (en) * | 2009-03-23 | 2010-06-16 | 江苏工业学院 | Oil and gas recovery device by absorption and adsorption integration technology |
| CN102441313A (en) * | 2010-10-12 | 2012-05-09 | 中国石油化工股份有限公司 | Oil gas recovery method |
| CN104815524A (en) * | 2015-04-09 | 2015-08-05 | 北京信诺海博石化科技发展有限公司 | Recovery technology for chemicals oil gas or mixed oil gas of chemicals and oil product |
| CN207749076U (en) * | 2017-12-06 | 2018-08-21 | 北京华清微拓节能技术股份公司 | A kind of refinery product's upgrading synergy and hydrogen recovery system |
| CN113136246A (en) * | 2020-01-17 | 2021-07-20 | 北京航天石化技术装备工程有限公司 | High-temperature garbage dry distillation oil-gas separation system and method |
| CN111569613A (en) * | 2020-05-26 | 2020-08-25 | 唐山三友硅业有限责任公司 | Device and method for eluting trace siloxane in organic silicon hydrolyzed HCl gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115678589A (en) * | 2022-11-18 | 2023-02-03 | 青岛飞普思环保科技有限公司 | Oil absorption process for oil gas recovery in light oil loading process |
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