CN218710221U - Oil field atmospheric gas is retrieved and is dehydrated, takes off heavy hydrocarbon, demercuration system - Google Patents
Oil field atmospheric gas is retrieved and is dehydrated, takes off heavy hydrocarbon, demercuration system Download PDFInfo
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- CN218710221U CN218710221U CN202222896855.XU CN202222896855U CN218710221U CN 218710221 U CN218710221 U CN 218710221U CN 202222896855 U CN202222896855 U CN 202222896855U CN 218710221 U CN218710221 U CN 218710221U
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Abstract
The utility model relates to an oil field atmospheric gas is retrieved and is dehydrated, take off heavy hydrocarbon, demercuration system, including regeneration gas separator, the adsorption tower, the regeneration gas heater, the demercuration tower, the dust filter, the regeneration gas cooler, the regeneration gas pipeline, still be provided with first three-way pipe, the second three-way pipe, regeneration gas separator liquid level control valve and 12 control valves, the adsorption tower is by compound adsorption tower one, compound adsorption tower two, supplementary adsorption tower is constituteed, regeneration gas separator includes first cavity and second cavity, first regeneration air control valve, first three-way pipe, the third is regenerated the air control valve and is established ties in proper order and constitute first branch road, second regeneration air control valve, the second three-way pipe, the fourth is regenerated the air control valve and is established ties in proper order and constitutes the second branch road, first branch road and second branch road are parallelly connected in the regeneration gas pipeline. The application forms multiple optional working conditions, enriches the processing means and improves the processing effect. The application is provided with a regeneration gas cold dryer. This application operating mode is abundant various, and work efficiency is high, and the heavy hydrocarbon is handled more fully.
Description
Technical Field
The application relates to an oil field atmospheric gas recovery and dehydration, take off heavy hydrocarbon, demercuration system mainly is applicable to the recovery and the purification utilization of oil field atmospheric gas.
Background
The oil field atmospheric gas is a natural gas byproduct that oil field exploitation oil in-process smugglied secretly, and its important composition is hydrocarbons such as methane, ethane, propane, butane, because its tolerance is unstable, and the tolerance of single-port well is less, and the piping transport degree of difficulty is big, is unfavorable for retrieving, so generally adopt the mode of directly discharging the ignition and burning out to handle in the oil exploitation before, not only wasted the natural gas resource, and the in-process of torch burning also can produce a large amount of harmful gas and greenhouse gas, can cause environmental pollution.
In recent years, more and more oil fields have come to notice this problem, and many oil field vent gas recovery devices are continuously built. In the existing oil field emptying gas purification system, the working process (working condition) 1 is simple, adsorption, regeneration and cold blowing cannot be continuously and simultaneously carried out, and the working efficiency is low; 2. regeneration gas is through water-cooling or air-cooling to about 40 ℃ after, does not have further cooling, and regeneration gas gets back to the adsorption tower bottom again, and the water content that wherein carries is more and takes the heavy hydrocarbon, has increased the load of molecular sieve, is unfavorable for getting rid of the heavy hydrocarbon as early as possible, and when mixing with the feed gas easily appears liquid in adsorption tower bottom, has slowed down the heating regeneration rate of adsorption tower.
Disclosure of Invention
The first technical problem solved by the application is to enrich the working condition process and improve the working efficiency; the second technical problem that this application solved is that early as far as possible clears up heavy hydrocarbon.
The technical solution adopted by the present application to solve the first technical problem is: the utility model provides an oil field atmospheric gas is retrieved and is dehydrated, take off heavy hydrocarbon, demercuration system, including regeneration gas separator, the adsorption tower, the regeneration gas heater, the demercuration tower, the dust filter, the regeneration gas cooler, the regeneration gas pipeline, the feed gas entry and regeneration gas pipeline, separator feed gas inlet connection, the regeneration gas pipeline is connected to separator regeneration gas entry through the regeneration gas cooler, the gaseous export of separator is connected with the adsorption tower, adsorption tower and regeneration gas heater, the demercuration tower is connected respectively, the regeneration gas heater is connected with the regeneration gas cooler, the demercuration tower is connected with the dust filter, characterized by: the composite adsorption tower comprises a first composite adsorption tower I, a second composite adsorption tower II and an auxiliary adsorption tower, the regeneration gas separator comprises a first cavity and a second cavity, the first regeneration gas control valve, the first three-way pipe and the fourth regeneration gas control valve are sequentially connected in series to form a second branch, the first regeneration gas control valve, the first three-way pipe and the third regeneration gas control valve are connected in parallel in a regeneration gas pipeline, and a cooling gas outlet is connected in parallel with a regeneration gas cooling pipeline; the bottom of the first chamber is provided with a liquid level regulating valve of the regeneration gas separator; the gas outlet of the separator at the top of the regeneration gas separator is respectively connected with the bottom of the first compound adsorption tower and the bottom of the second compound adsorption tower through the first compound adsorption tower inlet raw material gas control valve and the second compound adsorption tower inlet raw material gas control valve; a regenerated gas heating outlet or a blowing cooling inlet control valve of the composite adsorption tower is connected between the bottom of the first composite adsorption tower and the first three-way pipe, a regenerated gas heating inlet or a blowing cooling outlet control valve of the composite adsorption tower is connected between the top of the first composite adsorption tower and the top of the regenerated gas heater, a regenerated gas heating outlet or a blowing cooling inlet control valve of the second composite adsorption tower is connected between the bottom of the second composite adsorption tower and the first three-way pipe, and a regenerated gas heating inlet or a blowing cooling outlet control valve of the second composite adsorption tower is connected between the top of the second composite adsorption tower and the top of the regenerated gas heater. Through the above design, this application has greatly enriched the three adsorption tower of this application and has adsorbed respectively, regeneration, cold blowing and the operating mode kind and the technological means of mutually supporting, has realized adsorbing in succession simultaneously, regeneration, cold blowing, has improved rate of equipment utilization.
The technical solution adopted by the present application to solve the second technical problem is: the application still is provided with the cold machine of doing of regeneration gas, and the cold machine of doing of regeneration gas is installed between regeneration gas cooler and separator regeneration gas entry. Because the gas temperature after the regeneration gas cold dryer is used for processing is lower, the hydrocarbon-containing condensate can be analyzed after being uniformly mixed with the raw gas, the hydrocarbon-containing condensate enters the first cavity through the filter wire net and is discharged through the liquid level regulating valve of the regeneration gas separator, the hydrocarbon-containing condensate cannot enter the adsorption tower, the burden of the molecular sieve of the adsorption tower is reduced, the influence on the regeneration heating efficiency of the adsorption tower is reduced, and the burden of subsequent equipment for removing heavy hydrocarbon is reduced.
This application still is provided with regeneration gas flow control valve, and the feed gas entry is connected through regeneration gas flow control valve and separator feed gas entry, conveniently adjusts feed gas flow.
The temperature of the gas treated by the regeneration gas cool drying machine is 5-15 ℃, so that the heavy hydrocarbon condensation capacity of the regeneration gas separator is improved.
Ceramic balls, alumina, 4A molecular sieves and heavy hydrocarbon removal activated carbon are all filled in the composite adsorption tower I, the composite adsorption tower II and the auxiliary adsorption tower, and adsorption treatment capacity and efficiency are improved.
Compared with the prior art, the application has the following advantages and effects: the working condition flow is rich and diverse, the working efficiency is high, and the heavy hydrocarbon treatment is more sufficient.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present application.
In the figure: 1A-a first composite adsorption tower; 1B-a second composite adsorption tower; 2-an auxiliary adsorption tower; 3-demercuration tower; 4-a regeneration gas heater; 5-a dust filter; 6-regeneration gas cooler; 7-regeneration gas cooling and drying machine; 8-regeneration of the gas separator; 81-first chamber of the regenerative gas separator; 82-a second chamber of the regenerative gas separator; 83-filtering wire mesh; 84-wire mesh demister; 85-separator feed gas inlet; 86-separator regeneration gas inlet; 87-separator gas outlet; 88-a separator liquid outlet; 9-a regeneration gas pipeline; 91-parallel input port, 92-parallel output port, 93-first tee between first regeneration control valve K9 and third regeneration control valve K11; 94-second tee between second regeneration control valve K10 and fourth regeneration control valve K12, 10-feed gas inlet.
F1-a regenerated gas flow regulating valve; l1-a liquid level regulating valve of a regenerative gas separator; k1-the compound adsorption tower I is imported the raw materials air control valve; a K2-composite adsorption tower II inlet raw material gas control valve; k3-raw material gas control valve at the first outlet of the composite adsorption tower; k4-the raw material gas control valve at the second outlet of the composite adsorption tower; a regenerated gas heating outlet or a blowing cooling inlet control valve of the K5-composite adsorption tower; a control valve for a secondary regenerated gas heating outlet or a blowing cooling inlet of the K6-composite adsorption tower; a regenerated gas heating inlet or a blowing cooling outlet control valve of the K7-composite adsorption tower; a control valve for a heating inlet or a cooling outlet of the regenerated gas of the K8-composite adsorption tower II; k9-first regeneration control valve; k10-a second regeneration control valve; k11-a third regeneration control valve; k12-fourth regeneration control valve.
Detailed Description
The present application will be described in further detail below with reference to the accompanying drawings by way of examples, which are illustrative of the present application and are not limited to the following examples.
Referring to fig. 1, the system for recovering and dehydrating oil field vent gas, removing heavy hydrocarbons and removing mercury in the embodiment of the application is used for purifying the deacidified oil field vent gas, and can adsorb components such as moisture, C6+ heavy hydrocarbons and mercury in the oil field vent gas.
This embodiment can become the sled (indicate can wholly make into a sled, convenient removal) preparation, including following equipment: the device comprises a first compound adsorption tower 1A, a second compound adsorption tower 1B, an auxiliary adsorption tower 2, a demercuration tower 3, a regenerated gas heater 4, a dust filter 5, a regenerated gas cooler 6, a regenerated gas cooling dryer 7, a regenerated gas separator 8 and a regenerated gas pipeline 9, wherein the regenerated gas pipeline 9 is arranged on a raw gas inlet 10, a first regenerated gas control valve K9, a first three-way pipe 93 and a third regenerated gas control valve K11 are sequentially connected in series to form a first branch, a second regenerated gas control valve K10, a second three-way pipe 94 and a fourth regenerated gas control valve K12 are sequentially connected in series to form a second branch, the first branch and the second branch are connected in parallel in the regenerated gas pipeline 9, and a proper treatment flow can be selected according to actual conditions through the switching states of the 12 control valves (K1-K12). A part of raw gas is communicated through a parallel input port 91 of a regeneration gas pipeline 9, and a parallel output port 92 is communicated to a first chamber 81 of a regeneration gas separator 8 through a regeneration gas cooler 6, a regeneration gas cold dryer 7 and a separator regeneration gas inlet 86; the other part of the raw gas is communicated with a second chamber 82 at the upper part of the regeneration gas separator 8 through a regeneration gas flow regulating valve F1 and a separator raw gas inlet 85, a first chamber 81 of the regeneration gas separator 8 is arranged at the lower part of the regeneration gas separator 8, a regeneration gas separator liquid level regulating valve L1 is arranged at the bottom of the first chamber 81, and the regeneration gas separator liquid level regulating valve L1 is used for controlling the output of the treated heavy hydrocarbon and water; a gas outlet 87 of a separator at the top of the regeneration gas separator 8 is communicated with the bottom of a first compound adsorption tower 1A and the bottom of a second compound adsorption tower 1B through a first compound adsorption tower inlet raw material gas control valve K1 and a second compound adsorption tower inlet raw material gas control valve K2 respectively, the top of the first compound adsorption tower 1A is communicated with an inlet at the top of a demercuration tower 3 through a first compound adsorption tower 1A outlet raw material gas control valve K3, the top of the second compound adsorption tower 1B is communicated with an inlet at the top of the demercuration tower 3 through a second compound adsorption tower 1B outlet raw material gas control valve K4, an outlet at the bottom of the demercuration tower 3 is communicated with an inlet of a dust filter 5, gas treated by the dust filter 5 is discharged into a subsequent natural gas treatment process (such as liquefaction) from the outlet, the top of the first compound adsorption tower 1A is communicated with the top of a regeneration gas heater 4 through a first compound adsorption tower 1A regeneration gas heating inlet or a blowing and cooling outlet control valve K7, the top of the second compound adsorption tower 1B is communicated with the top of the regeneration gas heater 4 through a three-way pipe 94; the first 1A regenerated gas heating outlet or the blowing cooling inlet control valve K5 of the composite adsorption tower is connected between the bottom of the first 1A composite adsorption tower and the first three-way pipe 93, the first 1A regenerated gas heating inlet or the blowing cooling outlet control valve K7 of the composite adsorption tower is connected between the top of the first 1A composite adsorption tower and the top of the regenerated gas heater 4, the second 1B regenerated gas heating outlet or the blowing cooling inlet control valve K6 of the composite adsorption tower is connected between the bottom of the second 1B composite adsorption tower and the first three-way pipe 93, and the second regenerated gas heating inlet or the blowing cooling outlet control valve K8 of the composite adsorption tower is connected between the top of the second 1B composite adsorption tower and the top of the regenerated gas heater 4.
The parallel output port 92 is communicated with the first cavity 81 of the regeneration gas separator 8 through the regeneration gas cooler 6, the regeneration gas dryer 7 and the separator regeneration gas inlet 86, after the gas-liquid separation treatment is carried out through the regeneration gas separator 8, the liquid part is remained in the first cavity 81 of the regeneration gas separator 8, the discharge utilization or the further treatment can be controlled through the regeneration gas separator liquid level regulating valve L1, the gas part enters the second cavity 82 through the filtering wire mesh 83 of the regeneration gas separator 8, the gas part from the regeneration gas dryer 7 has lower temperature and is uniformly mixed with the raw gas from the separator raw gas inlet 85, so that the temperature of the raw gas is reduced to generate a certain condensed liquid containing hydrocarbon, the gas-liquid separation is carried out in the second cavity 82, the gas phase (gas) is treated through the wire mesh demister 84 at the upper part of the regeneration gas separator 8 and then is discharged from the separator gas outlet 87, the condensed liquid containing hydrocarbon enters the first cavity 81 through the filtering wire mesh 83 and is discharged through the regeneration liquid level regulating valve L1 and enters the subsequent other treatments, and does not enter the adsorption tower, the burden is reduced, and the influence on the heating efficiency of the adsorption tower molecular sieve.
The adsorption tower at least comprises three adsorption towers, including a first composite adsorption tower 1A, a second composite adsorption tower 1B and an auxiliary adsorption tower 2; the three adsorption towers are filled with fillers such as ceramic balls, alumina, a 4A molecular sieve, heavy hydrocarbon removal activated carbon and the like; during the same time period, at least the following four conditions exist, the first: the first composite adsorption tower 1A adsorbs raw material gas, the second composite adsorption tower 1B performs heating regeneration, and the auxiliary adsorption tower 2 adsorbs regenerated gas and cools the regenerated gas. And the second method comprises the following steps: the first composite adsorption tower 1A adsorbs the feed gas, the second composite adsorption tower 1B cools, and the auxiliary adsorption tower 2 heats and regenerates; and the third is that: the first composite adsorption tower 1A is used for heating and regenerating, the second composite adsorption tower 1B is used for adsorbing the feed gas, and the auxiliary adsorption tower 2 is used for adsorbing the regenerated gas and cooling the regenerated gas; and fourthly: the first composite adsorption tower 1A is used for cooling, the second composite adsorption tower 1B is used for adsorbing the feed gas, and the auxiliary adsorption tower 2 is used for heating and regenerating. Through the above design, this application has greatly enriched the three adsorption tower of this application and has adsorbed respectively, regeneration, blow the cold and operating mode kind and the technological means of mutually supporting, has realized adsorbing in succession simultaneously, regeneration, cold blowing, improve equipment utilization rate.
The following is a detailed description of the first operating mode:
the feed gas after 8 processes of regenerative gas separator comes out from separator gas outlet 87, and import raw materials air control valve K1 through composite adsorption tower gets into composite adsorption tower 1A and adsorbs, deviates from heavy hydrocarbon and water, gets into demercuration tower 3 through composite adsorption tower export raw materials air control valve K3 afterwards, accomplishes the demercuration back, exports the natural gas of dehydration, heavy hydrocarbon, demercuration through dust filter 5, gets into next step flow (for example liquefaction).
At this time, the second hybrid adsorption column 1B is undergoing the regeneration process. The regeneration process of the second composite adsorption tower 1B comprises two sub-processes of regeneration heating and cold blowing (cooling).
Regeneration and heating: a part of raw gas enters the auxiliary adsorption tower 2 through a regenerated gas pipeline 9, passes through a second regenerated gas control valve K10 and a second three-way pipe 94 for adsorption, is heated to 200-220 ℃ through a regenerated gas heater 4, enters the composite adsorption tower II 1B through a composite adsorption tower II regenerated gas heating inlet or a blowing and cooling outlet control valve K8 to analyze adsorbed water and heavy hydrocarbon, is discharged through a composite adsorption tower II outlet raw material gas control valve K6, enters the regenerated gas cooler 6 through a first three-way pipe 93 and a third regenerated gas control valve K11 to be cooled to about 40 ℃, enters the regenerated gas cold dryer 7, is further cooled to about 10 ℃, finally enters the regenerated gas separator 8 to separate water and heavy hydrocarbons, is mixed with the raw gas from a separator raw gas inlet 85, and then enters the composite adsorption tower I1A. And stopping heating when the temperature of the gas discharged from the second composite adsorption tower 1B in the regenerative heating process reaches 160-180 ℃, namely finishing the regenerative heating of the second composite adsorption tower 1B.
And (3) cold blowing: a part of raw material gas is used as regeneration gas, passes through a first regeneration gas control valve K9, a first three-way pipe 93 and a composite adsorption tower second outlet raw material gas control valve K6 through a regeneration gas pipeline 9, enters a composite adsorption tower second 1B from the bottom, reduces the temperature of the adsorbent in the tower to normal temperature, enters a regeneration gas heater 4 through a composite adsorption tower second regeneration gas heating inlet or a blowing cooling outlet control valve K8, is heated to 200-220 ℃, enters an auxiliary adsorption tower 2, heats and regenerates the adsorbent therein, is discharged from a fourth regeneration gas control valve 12 through a second three-way pipe 94, is cooled to about 40 ℃ through a regeneration gas cooler 6, enters a regeneration gas cold-dry separator 7, is cooled to about 10 ℃, and finally enters a regeneration gas cold-dry separator 8 to separate water and heavy hydrocarbons and the like and then enters the composite adsorption tower first 1A. When the temperature of the gas discharged from the second composite adsorption tower 1B reaches 160-180 ℃, the heating is stopped, namely, the regeneration heating of the auxiliary adsorption tower 2 is completed, at the moment, the second composite adsorption tower 1B is switched to an adsorption mode, the first composite adsorption tower 1A is switched to a regeneration mode, and the process is circulated.
The relevant switch states corresponding to the working conditions (modes) of the embodiment are referred to the following working state table, wherein the symbols in the table are as follows: a-adsorption (drying); h-regenerative heating; c, blowing for cooling; ON-valve open; switches not labeled ON are all off.
The second working condition is as follows: the first composite adsorption tower 1A adsorbs feed gas, the second composite adsorption tower 1B cools, and the auxiliary adsorption tower 2 regeneratively heats;
the third working condition is as follows: the first composite adsorption tower 1A carries out regeneration heating, the second composite adsorption tower 1B carries out adsorption on the feed gas, and the auxiliary adsorption tower 2 carries out adsorption on the regenerated gas and cools the regenerated gas;
the fourth working condition is as follows: the first composite adsorption tower 1A is cooled, the second composite adsorption tower 1B is used for adsorbing the feed gas, and the auxiliary adsorption tower 2 is used for regenerating and heating.
The main working process of the embodiment includes: the deacidified raw gas enters the embodiment, one part of the raw gas is used as the regeneration gas, the other part of the raw gas enters the second cavity 82 of the regeneration gas separator 8 through a regeneration gas flow regulating valve F1, after being mixed with the separated regeneration gas in the equipment, the mixture enters the first composite adsorption tower 1A from the top of the regeneration gas separator 8 through a first composite adsorption tower inlet raw material gas control valve K1, the water and the C6+ heavy hydrocarbon are adsorbed through a packing layer, the mixture is discharged from the top of the first composite adsorption tower 1A, then passes through a first composite adsorption tower outlet raw material gas control valve K3, enters the top of the demercuration tower 3, passes through the sulfur-leaching activated carbon, passes through a dust filter 5 after coming out from the bottom, and the purified oil field vent gas passes through a subsequent liquefaction system after being detected to be qualified; the regeneration gas enters the auxiliary adsorption tower 2 in sequence through a second regeneration gas control valve K10, a regeneration gas heater 4 is heated to a certain temperature, enters the composite adsorption tower II 1B from the top through a composite adsorption tower II regeneration gas heating inlet or a blowing cooling outlet control valve K8 to regenerate the filler in the tower, comes out from the bottom of the tower after regeneration, sequentially passes through a composite adsorption tower II regeneration gas heating outlet or a blowing cooling inlet control valve K6, a third regeneration gas control valve K11, a regeneration gas cooler 6 and a regeneration gas cooling dryer 7 and is cooled to a certain temperature, enters a first cavity 81 of a regeneration gas separator 8, is mixed with the main path feed gas in a second cavity 82 after gas-liquid separation, and closed circulation is formed.
In addition, it should be noted that the specific embodiments described in the present specification, the device names, etc. may be different, and the above contents described in the present specification are only illustrations of the structures of the present invention. All the equivalent changes or simple changes made according to the structure, characteristics and principle of the utility model are included in the protection scope of the utility model.
Claims (5)
1. The utility model provides an oil field atmospheric gas is retrieved and is dehydrated, take off heavy hydrocarbon, demercuration system, including regeneration gas separator, the adsorption tower, the regeneration gas heater, the demercuration tower, the dust filter, the regeneration gas cooler, the regeneration gas pipeline, the feed gas entry and regeneration gas pipeline, separator feed gas inlet connection, the regeneration gas pipeline is connected to separator regeneration gas entry through the regeneration gas cooler, the gaseous export of separator is connected with the adsorption tower, adsorption tower and regeneration gas heater, the demercuration tower is connected respectively, the regeneration gas heater is connected with the regeneration gas cooler, the demercuration tower is connected with the dust filter, characterized by: the composite adsorption tower comprises a first composite adsorption tower I, a second composite adsorption tower II and an auxiliary adsorption tower, the regeneration gas separator comprises a first cavity and a second cavity, the first regeneration gas control valve, the first three-way pipe and the fourth regeneration gas control valve are sequentially connected in series to form a second branch, the first regeneration gas control valve, the first three-way pipe and the third regeneration gas control valve are connected in parallel in a regeneration gas pipeline, and a cooling gas outlet is connected in parallel with a regeneration gas cooling pipeline; the bottom of the first chamber is provided with a liquid level regulating valve of the regeneration gas separator; the gas outlet of the separator at the top of the regeneration gas separator is respectively connected with the bottom of the first composite adsorption tower and the bottom of the second composite adsorption tower through a first composite adsorption tower inlet raw material control valve and a second composite adsorption tower inlet raw material control valve; a regenerated gas heating outlet or a blowing cooling inlet control valve of the composite adsorption tower is connected between the bottom of the first composite adsorption tower and the first three-way pipe, a regenerated gas heating inlet or a blowing cooling outlet control valve of the composite adsorption tower is connected between the top of the first composite adsorption tower and the top of the regenerated gas heater, a regenerated gas heating outlet or a blowing cooling inlet control valve of the second composite adsorption tower is connected between the bottom of the second composite adsorption tower and the first three-way pipe, and a regenerated gas heating inlet or a blowing cooling outlet control valve of the second composite adsorption tower is connected between the top of the second composite adsorption tower and the top of the regenerated gas heater.
2. The oil field vent gas recovery and dehydration, heavy hydrocarbon removal and mercury removal system of claim 1, characterized by: the device is also provided with a regenerated gas cooling and drying machine which is arranged between the regenerated gas cooler and the regenerated gas inlet of the separator.
3. The oil field vent gas recovery and dehydration, heavy hydrocarbon removal and mercury removal system of claim 1, wherein the system comprises: the device is also provided with a regenerated gas flow regulating valve, and the feed gas inlet is connected with the feed gas inlet of the separator through the regenerated gas flow regulating valve.
4. The oil field vent gas recovery and dehydration, heavy hydrocarbon removal and mercury removal system of claim 1, characterized by: the temperature of the gas after the treatment of the regeneration gas cooling dryer is between 5 and 15 degrees.
5. The oil field vent gas recovery and dehydration, heavy hydrocarbon removal and mercury removal system of any one of claims 1 to 4, characterized by: ceramic balls, alumina, a 4A molecular sieve and heavy hydrocarbon removal activated carbon are filled in the first composite adsorption tower, the second composite adsorption tower and the auxiliary adsorption tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222896855.XU CN218710221U (en) | 2022-11-01 | 2022-11-01 | Oil field atmospheric gas is retrieved and is dehydrated, takes off heavy hydrocarbon, demercuration system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222896855.XU CN218710221U (en) | 2022-11-01 | 2022-11-01 | Oil field atmospheric gas is retrieved and is dehydrated, takes off heavy hydrocarbon, demercuration system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116836742A (en) * | 2023-07-31 | 2023-10-03 | 合肥万豪能源设备有限责任公司 | High-sulfur natural gas purifying and sulfur recycling system |
| CN117165346A (en) * | 2023-10-27 | 2023-12-05 | 陕西航天德林科技集团有限公司 | Natural gas dehydration and mercury removal method |
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2022
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116836742A (en) * | 2023-07-31 | 2023-10-03 | 合肥万豪能源设备有限责任公司 | High-sulfur natural gas purifying and sulfur recycling system |
| CN117165346A (en) * | 2023-10-27 | 2023-12-05 | 陕西航天德林科技集团有限公司 | Natural gas dehydration and mercury removal method |
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