CN114011208B - Gasoline and oil gas recovery device - Google Patents
Gasoline and oil gas recovery device Download PDFInfo
- Publication number
- CN114011208B CN114011208B CN202111231984.0A CN202111231984A CN114011208B CN 114011208 B CN114011208 B CN 114011208B CN 202111231984 A CN202111231984 A CN 202111231984A CN 114011208 B CN114011208 B CN 114011208B
- Authority
- CN
- China
- Prior art keywords
- gasoline
- inlet
- gas
- absorber
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000011084 recovery Methods 0.000 title claims abstract description 40
- 238000001179 sorption measurement Methods 0.000 claims abstract description 69
- 239000003463 adsorbent Substances 0.000 claims abstract description 56
- 239000002250 absorbent Substances 0.000 claims abstract description 52
- 230000002745 absorbent Effects 0.000 claims abstract description 52
- 238000010521 absorption reaction Methods 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 14
- 238000012806 monitoring device Methods 0.000 claims abstract description 14
- 230000001105 regulatory effect Effects 0.000 claims abstract description 12
- 230000008929 regeneration Effects 0.000 claims abstract description 10
- 238000011069 regeneration method Methods 0.000 claims abstract description 10
- 238000001514 detection method Methods 0.000 claims abstract description 9
- 238000011282 treatment Methods 0.000 claims abstract description 9
- 238000004891 communication Methods 0.000 claims abstract description 8
- 238000012544 monitoring process Methods 0.000 claims abstract description 4
- 239000006096 absorbing agent Substances 0.000 claims description 49
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 21
- 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
- 238000000034 method Methods 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 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
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Classifications
-
- 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
-
- 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
-
- 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 present disclosure provides a gasoline vapor recovery apparatus including an absorption tower for countercurrent contacting an absorbent, which is accessed through an absorbent inlet, and gasoline vapor, which is accessed through a gasoline vapor inlet, in an up-down direction to make the absorbent absorb gasoline in the gasoline vapor, a coalescer, an adsorption apparatus, a vacuum pump, a temperature monitoring apparatus, an emission concentration detection apparatus, and a temperature adjustment apparatus; the coalescer is used for receiving the gasoline and oil gas treated by the absorbent of the absorption tower and further separating the gas and the liquid of the coalescer; the adsorption device is provided with an adsorbent, and the adsorbent is used for adsorbing the gas carrying the residual gasoline moving from bottom to top; the vacuum pump is used for carrying out vacuum regeneration on the adsorbent; the temperature regulating device is in communication connection with the discharge concentration detecting device and the temperature monitoring device and adjusts the temperature of the external absorbent. And (3) carrying out three times of gasoline and oil gas treatment through the absorption tower, the coalescer and the adsorption device, so that the content of discharged gasoline-containing gas is reduced.
Description
Technical Field
The present disclosure relates to the field of oil and gas recovery, and more particularly to a gasoline oil and gas recovery apparatus.
Background
In the loading process of the oil product, oil gas generated by volatilization of the gasoline product is dissipated to the top of the tank car and discharged to the atmosphere, and the volatilized oil gas has the characteristics of inflammability and explosiveness, has high concentration, forms explosive gas with air and is distributed in the upper space of the tank car and around the loading exhaust port of the tank car, and is extremely easy to explode when encountering open fire, thereby influencing the safety production. For this reason, recovery of the volatilized oil and gas is required.
Although oil and gas recovery devices are currently provided for volatilized oil and gas, the emission concentration of discharged gasoline-containing gas after treatment by the oil and gas recovery devices is required to be lower and lower due to increasingly strict environmental requirements. Thus, it is necessary to further reduce the emission concentration of the gasoline-containing gas emitted after the recovery treatment, in order to be environmentally friendly.
Disclosure of Invention
In view of the problems in the background art, an object of the present disclosure is to provide a gasoline vapor recovery device capable of reducing the emission concentration of a gasoline-containing gas emitted after the treatment of the gasoline vapor recovery device.
Thus, in some embodiments, a gasoline vapor recovery device includes an absorber, a coalescer, an adsorption device, a vacuum pump, a temperature monitoring device, a discharge concentration detecting device, and a temperature adjusting device, the absorber is provided with an absorber inlet, a gasoline vapor inlet, and a discharge outlet, the absorber inlet is located above the gasoline vapor inlet, the discharge outlet is located above the absorber inlet, the absorber inlet is used for accessing an external absorber, the gasoline vapor inlet is used for accessing gasoline vapor of an external gasoline storage tank, the absorber is used for countercurrent contact in an up-down direction between the absorber accessed through the absorber inlet and the gasoline vapor accessed through the gasoline vapor inlet, so that the absorber absorbs gasoline in the gasoline vapor, the absorber absorbing the gasoline becomes rich liquid and falls and is collected in a lower portion of the absorber, and the discharge outlet is used for discharging the gasoline vapor treated by the absorber; 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 outlet of the absorption tower and is used for receiving gasoline and oil gas treated by the absorbent of the absorption tower and further separating gas and liquid of the coalescer, separated gasoline drops are collected at the lower part of the coalescer, and separated gas carrying residual gasoline is discharged through the first outlet; the adsorption device is provided with an inlet, a discharge port and an adsorbent, wherein the inlet is lower than the discharge port, the inlet of the adsorption device is controlled to be communicated with a first outlet of the coalescer and is used for receiving gas carrying residual gasoline from the coalescer, the adsorbent is arranged between the inlet and the discharge port along the up-down direction and is used for adsorbing gasoline of the gas carrying residual gasoline moving from bottom to top, and the discharge port is used for discharging the gas containing gasoline passing through the adsorbent; the vacuum pump is controlled to be communicated with the adsorption device and 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 an external absorbent and the temperature of external gasoline and oil gas; the emission concentration detection device is used for detecting the concentration of the gas containing gasoline discharged from the emission port of the adsorption device; the temperature regulating device is in communication connection with the emission concentration detection device and the temperature monitoring device, and the temperature regulating device regulates 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 gas and the concentration of the gasoline-containing gas emitted from the emission port of the adsorption device monitored by the emission concentration detection device.
In some embodiments, the absorbent is gasoline.
In some embodiments, the absorber 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 tank.
In some embodiments, the adsorption means are two and arranged in parallel, one for operation and the other as said one for adsorption and operation upon regeneration, such that the two adsorption means operate alternately.
In some embodiments, the adsorbents of the adsorbent device comprise a plurality of adsorbents that differ in their operating life under the adsorption conditions, the plurality of adsorbents being arranged from bottom to top in terms of the type of adsorbent and the operating life, the type of adsorbent with the longest operating life being placed closest to the inlet side, the second longest operating life being the type of adsorbent, and so on.
In some embodiments, the adsorbent of the adsorption device comprises silica gel and activated carbon, the silica gel being adjacent to the inlet relative to the activated carbon, and the activated carbon being adjacent to the discharge port 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 the gasoline vapor inlet of the absorber to supply vacuum regenerated gasoline from the adsorbent to the absorber.
In some embodiments, the temperature regulating device controls the temperature of the external absorbent to 3 ℃ to 5 ℃.
The beneficial effects of the present disclosure are as follows: in the gasoline vapor recovery apparatus according to the present disclosure, the three gasoline vapor treatments are performed by the absorption tower, the coalescer, the adsorption apparatus, so that the content of the gasoline-containing gas discharged from the discharge port of the adsorption apparatus is reduced, thereby satisfying further and more stringent environmental requirements.
Drawings
Fig. 1 shows a layout of a gasoline vapor recovery device according to the present disclosure.
Wherein reference numerals are as follows:
first outlet of 100 gasoline vapor recovery device 22
D up-down direction 23 second outlet
1 absorption tower 3 adsorption device
11 absorber inlet 31 inlet
12 gasoline gas inlet 32 discharge port
13 discharge port 4 vacuum pump
14 rich liquor outlet 5 temperature monitoring device
2 coalescer 6 discharge concentration detection device
21 first inlet 7 temperature regulating device
Detailed Description
The drawings illustrate embodiments of the present disclosure, and it is to be understood that the disclosed embodiments are merely examples of the disclosure that may be embodied in various forms and that, 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 practice the disclosure.
Referring to fig. 1, a gasoline vapor recovery system 100 includes an absorption tower 1, a coalescer 2, an adsorption device 3, a vacuum pump 4, a temperature monitoring device 5, a discharge concentration detection device 6, and a temperature adjustment device 7.
The absorber 1 is provided with an absorber inlet 11, a gasoline-gas inlet 12 and a discharge outlet 13, the absorber inlet 11 is positioned above the gasoline-gas inlet 12, the discharge outlet 13 is positioned above the absorber inlet 11, the absorber inlet 11 is used for being connected with an external absorber, the gasoline-gas inlet 12 is used for being connected with gasoline gas of an external gasoline storage tank, the absorber 1 is used for enabling the absorber connected through the absorber inlet 11 and the gasoline gas connected through the gasoline-gas inlet 12 to be in countercurrent contact in the up-down direction D so that the absorber absorbs gasoline in the gasoline gas, the absorber absorbing the gasoline becomes rich liquid to fall and is collected at the lower part of the absorber 1, and the discharge outlet 13 is used for discharging the gasoline gas treated by the absorber;
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 outlet 13 of the absorption tower 1 and is used for receiving gasoline and oil gas after absorbent treatment of the absorption tower 1 and further separating gas and liquid of the coalescer 2, separated gasoline 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 has an inlet 31, a discharge port 32, and an adsorbent, the inlet 31 being lower than the discharge port 32, the inlet 31 of the adsorption device 3 being in controlled communication with the first outlet 22 of the coalescer 2 and for receiving residual gasoline-carrying gas from the coalescer 2, the adsorbent being disposed between the inlet 31 and the discharge port 32 in the up-down direction D and for adsorbing gasoline-carrying gas moving from below to above, and the discharge port 32 for discharging gasoline-carrying 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 for adsorbing 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 gas.
The discharge concentration detection means 6 is for detecting the concentration of the gasoline-containing gas discharged from the discharge port 32 of the adsorption means 3.
The temperature adjusting device 7 is communicatively connected to the exhaust 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 gas, and the concentration of the gasoline-containing gas exhausted from the exhaust port 32 of the adsorbing device 3 monitored by the exhaust concentration detecting device 6.
In the gasoline vapor recovery apparatus 100 according to the present disclosure, the three gasoline vapor treatments are performed by the absorption tower 1, the coalescer 2, and the adsorption apparatus 3, so that the content of the gasoline-containing gas discharged from the discharge port 32 of the adsorption apparatus 3 is reduced, thereby satisfying the environmental requirements of further stricter (i.e., lower and lower discharge concentration).
The external gasoline storage tank to which the gasoline hydrocarbon inlet 12 is connected may come from a tank car or a tank farm.
In one example, the external absorbent to which the absorbent inlet 11 is connected is gasoline. By adopting the gasoline as the absorbent, the countercurrent absorption of gasoline and oil gas is more effective, and the gasoline recovered after being treated by the absorption tower 1 and the coalescer 2 can be directly returned to an external gasoline storage tank as described later, and the gasoline recovered after being treated by the vacuum pump 4 adopting the dry vacuum pump is directly returned to the absorption tower 1, so that the separation and recovery operation is not required like the operation of adopting the absorbent other than gasoline, 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 improved.
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 part of gasoline is directly recovered to an external gasoline storage tank through a rich liquid outlet 14, so that the quantity of the gasoline delivered to the outside of the external gasoline storage tank is increased.
Likewise, referring to fig. 1, the coalescer 2 also has a second outlet 23, the second outlet 23 being provided in the lower part of the coalescer 2, the second outlet 23 being for a gasoline tank communicating with the outside. In the coalescer 2, the gasoline droplets collected in the lower part of the coalescer 2 are pure gasoline in the case that the external absorbent is gasoline, and the part of the gasoline is directly recovered to the external gasoline tank through the second outlet 23, thereby increasing the amount of the gasoline shipped to the outside of the external gasoline tank.
In the example shown in fig. 1, the adsorption means 3 are provided in two and in parallel, one of the adsorption means 3 is used for operation, and the other adsorption means 3 is used as the one adsorption means 3 to complete adsorption and operate at the time of regeneration, so that the two adsorption means 3 alternately operate. Because the adsorbent of the adsorption device 3 is loaded in the adsorption device 3, unlike the continuous connection of the adsorbent of the adsorption 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 continuous working time of the gasoline vapor recovery device 100 is prolonged by adopting the arrangement of the two adsorption devices 3, so that the working pause of the gasoline vapor recovery device 100 caused by stopping the operation because the regeneration of the adsorbent of the adsorption device 3 due to the fact that only one adsorption device 3 is adopted is completed is avoided. Of course, the number of adsorption means 3 may be more than two.
Since the adsorbent device 3 is operated with different loads of the adsorbent from the inlet 31 to the discharge 32, the adsorbent at the inlet 31 is saturated earlier than the adsorbent at the discharge 32, and the whole stop of the adsorbent device 3 is usually based on the saturation of the adsorbent at the inlet 31, whereby, in order to overcome the difference in saturation of the adsorbent from the inlet 31 to the discharge 32 of the adsorbent device 3 with the continuation of the adsorption process, the adsorbent of the adsorbent device 3 comprises a plurality of adsorbents having different service lives under the adsorption conditions, the plurality of adsorbents are arranged from bottom to top in accordance with the kind and service life of the adsorbent, the kind of the adsorbent having the longest service life is placed closest to the inlet 31 side, the kind of the adsorbent having the second longest service life is placed next, and so on. Thereby enabling the various adsorbents to reach saturation as much as possible at the same time as the adsorption process continues. This not only allows the various adsorbents to function sufficiently and completely, but also allows the adsorption effect to be in a constant state (i.e., fully saturated from fresh charge) throughout the operation of the adsorption apparatus 3 before regeneration, which is advantageous in that the concentration of the gasoline-containing gas discharged from the discharge port 32 of the adsorption apparatus 3 is relatively uniform during the long-term operation of the gasoline vapor recovery apparatus 100, thereby improving the stability of the discharge quality during the long-term operation of the vapor recovery apparatus 100.
In one example, the adsorbent of the adsorption device 3 comprises 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 discharge 32 relative to the silica gel.
In one example, the vacuum pump 4 is a dry vacuum pump. In contrast to working media using oil, water or other polymeric media as the pump, the dry vacuum pump uses only air and no oil, water or other polymeric media, so that the gasoline recovered when the dry vacuum pump regenerates the adsorbent of the adsorption device 3 by vacuuming does not contain impurities carried by the media of the vacuum pump 4 itself. When the absorbent of the absorption tower 1 adopts gasoline, the recovered gasoline is gas-carried gasoline due to the vacuum-pumping of the dry vacuum pump 4, which is exactly identical in composition and morphology to the produced oil gas of the external gasoline reservoir, whereby further, in the example shown in the figure, the vacuum pump 4 is also communicated with the gasoline oil gas inlet 12 of the absorption tower 1 to supply the vacuum-recovered gasoline from the absorbent to the absorption tower 1. Thus, not only is the need for separate treatment of the gasoline recovered during the vacuuming regeneration of 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 improved. In the example shown in the figures, the temperature regulating device 7 is arranged directly on the line of the absorbent feed to the absorbent inlet 11 of the absorption tower 1. For example, the temperature adjusting device 7 adjusts the temperature of the absorbent by using a water jacket method. In other embodiments, the temperature regulating device 7 may be arranged adjacent to the line of the absorbent inlet 11 of the absorber 1 to which the absorbent is fed.
In one example, the temperature regulating device 7 controls the temperature of the external absorbent to 3-5 ℃. The temperature is too low (i.e. lower than 3 ℃), so that the fluidity of the gasoline becomes poor when the gasoline is used as an absorbent, which is unfavorable for the absorption of the gasoline in the gasoline gas when the gasoline as an absorbent is in countercurrent contact with the absorbent which is accessed through the absorbent inlet 11 and the gasoline gas which is accessed through the gasoline gas inlet 12 in the up-down direction D after entering the absorption tower 1, and the requirements of the temperature regulator 7 on equipment, media and the like for adjusting the absorbent at a lower temperature are increased (i.e. the lower the temperature is, the more demanding the requirements are); the temperature is too high (i.e., higher than 5 deg.c), and the gasoline as the absorbent may volatilize, which increases the amount of gasoline vapor on the basis of the gasoline vapor itself introduced through the gasoline vapor inlet 12, since the absorbent gasoline is introduced through the absorbent inlet 11 located above the gasoline vapor inlet 12, if the absorbent gasoline may volatilize, the part of the volatilized gasoline vapor from the absorbent is discharged to the coalescer 2 directly through the discharge outlet 13 located above the absorbent inlet 11 due to the inability to perform the aforementioned countercurrent adsorption, thereby reducing the adsorption effect of the absorber 1, and further, the discharge concentration of the gasoline-containing gas discharged through the discharge outlet 32 may be increased with the same coalescer 2 and adsorption device 3.
And finally, giving a test example.
Example 1
The whole structure and path arrangement of fig. 1 are adopted, the geometric similarity miniaturization test of the same proportion is carried out in a laboratory, and the operation condition of the whole gasoline oil gas recovery device is simulated through HYSYS. The absorbent adopts gasoline, the absorbent of the adsorption device 3 adopts silica gel and active carbon, the silica gel is close to an inlet 31 relative to the active carbon, the active carbon is close to an exhaust port 32 relative to the silica gel, the vacuum pump 4 adopts a dry vacuum pump, the temperature of the gasoline serving as the absorbent is controlled at 3 ℃, and the temperature of the gasoline gas and the oil gas which is connected into a gasoline gas inlet 12 is 30 ℃ in summer.
The oil gas recovery efficiency reaches 98 percent, and the emission concentration is 8-13 g/m 3 Left and right.
And annex B of the emission standard of atmospheric pollutants in an oil storage warehouse in GB 20950-2007 of oil gas recovery efficiency.
Example 2
Example 1 was repeated except that the temperature of the gasoline as the absorbent was controlled to 5 ℃.
The oil gas recovery efficiency reaches 97 percent, and the emission concentration is 12-15 g/m 3 Left and right.
Comparative example 1
Only the coalescer of fig. 1 is omitted.
The oil gas recovery efficiency reaches 95, and the emission concentration is 20-25 g/m 3 Left and right.
Comparative example 2
The temperature of the gasoline as the absorbent alone was controlled at 2 deg.c, with the remainder being the same as in example 1.
The oil gas recovery efficiency reaches 96.5, and the emission concentration is 10-14g/m 3 Left and right.
Comparative example 3
The temperature of the gasoline as the absorbent alone was controlled at 6℃with the remainder of example 1.
The oil gas recovery efficiency reaches 96.5, and the emission concentration is 14-17g/m 3 Left and right.
The various exemplary embodiments are described using the above detailed description, but are not intended to be limited to the combinations explicitly disclosed herein. Thus, unless otherwise indicated, the various features disclosed herein may be combined together to form a number of additional combinations that are not shown for the sake of brevity.
Claims (10)
1. A gasoline and 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), a discharge concentration detection device (6) and a temperature regulating device (7),
the absorber (1) is provided with an absorber inlet (11), a gasoline-gas inlet (12) and a discharge outlet (13), the absorber inlet (11) is positioned above the gasoline-gas inlet (12), the discharge outlet (13) is positioned above the absorber inlet (11), the absorber inlet (11) is used for being connected with an external absorber, the gasoline-gas inlet (12) is used for being connected with gasoline gas of an external gasoline storage tank, the absorber (1) is used for enabling the absorber connected with the absorber through the absorber inlet (11) and the gasoline gas connected with the gasoline gas through the gasoline-gas inlet (12) to be in countercurrent contact in the up-down direction (D), so that the absorber absorbs gasoline in the gasoline gas, the absorber absorbing gasoline becomes rich liquid, falls and is collected at the lower part of the absorber (1), and the discharge outlet (13) is used for discharging the gasoline gas treated by the absorber;
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 outlet (13) of the absorption tower (1) and is used for receiving gasoline and oil gas after absorbent treatment of the absorption tower (1) and further separating gas from liquid of the coalescer (2), separated gasoline 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 controlled to be communicated with a first outlet (22) of the coalescer (2) and is used for receiving gas carrying residual gasoline from the coalescer (2), the adsorbent is arranged between the inlet (31) and the discharge outlet (32) along the up-down direction (D) and is used for adsorbing gasoline of the gas carrying residual gasoline moving from bottom to top, and the discharge outlet (32) is used for discharging the gas containing gasoline passing through the adsorbent;
the vacuum pump (4) is controlled to be communicated with the adsorption device (3) and is used for carrying out vacuum regeneration on the adsorbent of the adsorption device (3) for adsorbing gasoline;
the temperature monitoring device (5) is used for monitoring the ambient temperature, the temperature of an external absorbent and the temperature of external gasoline and oil gas;
the discharge 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 regulating device (7) is in communication connection with the emission concentration detecting device (6) and the temperature monitoring device (5), and the temperature regulating device (7) regulates 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 gas and the concentration of the gasoline-containing gas discharged from the emission port (32) of the adsorption device (3) monitored by the emission concentration detecting device (6).
2. The gasoline vapor recovery apparatus (100) of claim 1, wherein the absorbent is gasoline.
3. The gasoline vapor recovery apparatus (100) according to claim 2, wherein the absorption tower (1) further comprises a rich liquid outlet (14), the rich liquid outlet (14) being for communication with an external gasoline 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 provided in a lower portion of the coalescer (2), the second outlet (23) being for communication with an external gasoline tank.
5. The gasoline vapor recovery system (100) of claim 1, wherein,
the adsorption devices (3) are two and are arranged in parallel, one adsorption device (3) is used for working, and the other adsorption device (3) is used as one adsorption device (3) to finish adsorption and work in regeneration, so that the two adsorption devices (3) work alternately.
6. The gasoline vapor recovery system (100) of claim 2 wherein,
the adsorbents of the adsorption device (3) comprise a plurality of adsorbents, the working lives of the plurality of adsorbents under adsorption conditions are different, the plurality of adsorbents are arranged from bottom to top according to the types and the working lives of the adsorbents, the type of the adsorbent with the longest working life is arranged closest to the inlet (31), the type of the adsorbent with the second longest working life is arranged next, and so on.
7. The gasoline vapor recovery system (100) of claim 6, wherein the adsorbent of the adsorption device (3) comprises 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 discharge (32) relative to the silica gel.
8. The gasoline vapor recovery apparatus (100) of claim 2, wherein the vacuum pump (4) is a dry vacuum pump.
9. The gasoline vapor recovery apparatus (100) as defined in claim 8 wherein the vacuum pump (4) is further connected to the gasoline vapor inlet (12) of the absorber (1) to supply the vacuum regenerated gasoline from the adsorbent to the absorber (1).
10. A gasoline vapor recovery system (100) as claimed in claim 2 wherein the temperature regulating means (7) controls the temperature of the external absorbent to 3-5 ℃.
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 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111231984.0A CN114011208B (en) | 2021-10-22 | 2021-10-22 | Gasoline and oil gas recovery device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114011208A CN114011208A (en) | 2022-02-08 |
| CN114011208B true CN114011208B (en) | 2024-04-09 |
Family
ID=80057194
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111231984.0A Active CN114011208B (en) | 2021-10-22 | 2021-10-22 | Gasoline and oil gas recovery device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114011208B (en) |
Families Citing this family (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 |
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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114011208A (en) | 2022-02-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN114011208B (en) | Gasoline and oil gas recovery device | |
| CN205461670U (en) | Storage tank discharged waste gas's deep purification recovery unit | |
| CN106422667A (en) | Method for removing acidic components and water from gas in one step | |
| JP2014057941A (en) | Carbon dioxide separation and recovery system and carbon dioxide separation and recovery method | |
| CN1806894A (en) | Oil gas absorptive reclaiming method and apparatus | |
| CN103111084A (en) | Condensation-adsorption combined process capable of improving the service life of oil vapor recovery system equipment | |
| US5681369A (en) | Apparatus and method for recovering volatile liquid | |
| EP0628336B1 (en) | Vapor recovery system | |
| KR20140009270A (en) | Method for removing organic solvent, and removal device | |
| CN112657310A (en) | High-concentration tetrahydrofuran organic waste gas treatment process and device | |
| CN202226647U (en) | Oil gas recovering system for gas station | |
| CN201505500U (en) | Oil and gas recovery device by absorption and adsorption integration technology | |
| US5330563A (en) | Process for separating a volatile organic compound from a gas | |
| CN107854955B (en) | Hydrocarbon-containing waste gas recovery process and operation control method | |
| CN111471479B (en) | Oil absorption process for oil gas recovery | |
| CN104548879B (en) | A kind of oil plant sour water tank method for treating release gas and device | |
| CN110935281B (en) | Adsorption and regeneration device and method for solid adsorbent for adsorbing volatile organic compounds | |
| CN107737511A (en) | A kind of safety-type absorbent charcoal adsorption tank oil-gas recovery method | |
| CN102029100A (en) | Dry desorption process for activated carbon adsorption of organic waste gas | |
| CN102557862A (en) | Process for deoxidizing and dehydrating tetrachloroethylene and equipment for process | |
| CN112403200A (en) | Treatment process of styrene-containing waste gas | |
| CN205099633U (en) | Regenerating unit and one step of deacidification dewatering system | |
| CN203342421U (en) | Condensation adsorption system for improving service life of oil gas recovery system | |
| CN102527186A (en) | Technology and system for recycling solvent oil from oil gas of butadiene prepared from butane under oxidative dehydrogenation effect | |
| CN101947402B (en) | System and process for recovering butanol and butyl ester in penicillin industrial production waste gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |