CN113069891A - Oil gas recovery method - Google Patents
Oil gas recovery method Download PDFInfo
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- CN113069891A CN113069891A CN202110514603.3A CN202110514603A CN113069891A CN 113069891 A CN113069891 A CN 113069891A CN 202110514603 A CN202110514603 A CN 202110514603A CN 113069891 A CN113069891 A CN 113069891A
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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
- B01D53/1487—Removing organic compounds
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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
- B01D53/002—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 condensation
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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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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/04—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with liquid absorbents
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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Abstract
The invention discloses an oil gas recovery method. Comprises the following steps S1-S3 or S2-S3: s1, conveying heavy oil gas in oil gas to be recovered to a liquid separating tank I for gas-liquid separation, conveying the oil gas obtained by separation to an absorption tower from the bottom of the absorption tower, reversely absorbing the oil gas with an absorbent from the top of the absorption tower, discharging the oil gas from the top of the absorption tower, and then feeding the oil gas into a liquid separating tank II; s2, carrying out gas-liquid separation on light oil gas in the oil gas to be recovered and oil gas from the top of the absorption tower in a liquid separation tank II, and sequentially conveying the oil gas obtained by separation to a condenser I and a condenser II for condensation treatment; s3, conveying the non-condensable oil gas condensed in the step S2 to a liquid separating tank IV for gas-liquid separation, conveying the separated oil gas after reheating to an adsorption tank for adsorption treatment, and discharging the adsorbed tail gas after reaching the standard. The invention enables the oil gas to reach the standard to be discharged through three-stage process treatment of absorption, condensation and adsorption, and improves the oil gas treatment efficiency through separate collection of light oil gas and heavy oil gas.
Description
Technical Field
The invention relates to an oil gas recovery method, and belongs to the field of environmental protection.
Background
The petroleum chemical and coal chemical products inevitably produce oil evaporation in the processes of storage, transportation and the like, so that oil loss and oil gas pollution are caused. The oil gas contains various hydrocarbon organic compounds, and if the volatilized oil gas is not recycled, waste is generated and the environment is polluted. At present, the national strict regulation requirements on the emission of atmospheric pollutants, and the emission of oil gas must meet the emission standards regulated by the nation, so that the oil gas recovery must be carried out.
In the prior art, oil gas recovery mainly comprises technologies such as an absorption method, an adsorption method, a condensation method and a membrane separation method, and the most widely used method at present is an activated carbon adsorption method, and in addition, methods combining absorption + adsorption, condensation + adsorption and the like in pairs are also available, but various problems exist in the methods. The absorption method is a process for absorbing oil gas by using an absorbent by utilizing the principle of similar and compatible organic matters, generally has low efficiency, and can not reach the standard only by adopting the absorption method; the adsorption method is a process for adsorbing oil gas by using an adsorbent, and although the process is simple, the adsorption method cannot reach the standard; the condensation method is a process of condensing oil gas by a condensing agent through a heat exchanger and then recovering the oil gas, and has low condensation temperature and large energy consumption; the membrane separation method is a process for separating and recovering oil and gas by utilizing the selective permeability of a polymeric membrane, and the cost of the separation membrane is high and a certain concentration difference between two sides of the membrane needs to be maintained. The emission concentration of organic matter is not up to standard after the oil gas treatment, if the oil gas temperature of handling is too high, active carbon adsorption effect can descend to the adsorption process can make the active carbon temperature rise for exothermic process, and adsorption efficiency also can be reduced. The absorption and adsorption combined method generally has the problems of high energy consumption and substandard emission.
Chinese patent application CN 111876191 a discloses a novel combined oil gas recovery system and oil gas recovery method, the oil gas recovery system adopts two tanks, and desorption inlets and desorption outlets which are arranged on the side surfaces of the tanks uniformly and are horizontally opposite are utilized to make the desorption gas flow distribution in the horizontal direction more uniform, and the adsorption and desorption working modes of the two tanks are exchanged to realize the repeated circulation of oil gas adsorption and desorption. The method adopts a single adsorbent adsorption method, so that the discharge requirement is difficult to meet, the number of the openings of the adsorption tanks is large, and the number of the pipeline configurations is large. Chinese patent application CN 111575042 a discloses a combination oil gas recovery device and recovery process, the device utilizes two-stage absorption system and the adsorption system who comprises two adsorption tanks to separate oil gas and retrieve, the heavy hydrocarbon macromolecule in the earlier separation combination oil gas of circulation circuit through adsorption system and second absorption system formation, to light hydrocarbon micromolecule oil gas circulation repeated absorption again, the recovery efficiency of light hydrocarbon micromolecule oil gas is improved, the separation of realization combination oil gas is retrieved. The device comprises two oil depots and two absorption towers, occupies a large area, and needs to provide a large amount of oil gas absorbent. Chinese patent application CN 111151099 a discloses a process for low-temperature absorption of oil gas, which is an absorption and adsorption integration method based on a novel absorption tower, matched with a specific low-temperature absorbent, and adopting a full-flow system to control operation. The method needs to use a specific absorption tower and a specific absorbent, oil gas is discharged after being absorbed once and possibly does not reach the standard, the oil gas after being absorbed at low temperature is regenerated, condensed, compressed and condensed to recover part of oil products, and the process is redundant.
In summary, the existing methods all have different disadvantages, and a new oil gas recovery method needs to be provided.
Disclosure of Invention
The invention aims to provide a novel oil gas recovery method, which provides an improved oil gas recovery method with better economy through the optimized combination and process improvement of the prior art according to the characteristics of oil gas recovery.
The oil gas is discharged up to the standard through three-stage process treatment of absorption, condensation and adsorption, the oil gas treatment efficiency is improved through the separate collection of light oil gas and heavy oil gas, the temperature of heavy oil gas is high and the heavy oil gas is easy to condense, so that heavy components in the heavy oil gas are treated independently by using an absorbent in an absorption part, and the fully absorbed heavy oil gas enters a subsequent process for continuous treatment; and the light oil gas is condensed and then is recycled to be partially oil product, finally is discharged after reaching the standard through the adsorption part, and if the light oil gas is not up to the standard in the accident state, the light oil gas can be discharged to a torch in an interlocking control mode, so that the direct discharge of the light oil gas into the atmosphere is avoided.
The oil gas recovery method provided by the invention comprises the following steps S1-S3 or S2-S3:
s1, conveying heavy oil gas in oil gas to be recovered to a liquid separating tank I for gas-liquid separation, conveying the oil gas obtained by separation to an absorption tower from the bottom of the absorption tower, reversely absorbing the oil gas with an absorbent from the top of the absorption tower, discharging the oil gas from the top of the absorption tower, and then feeding the oil gas into a liquid separating tank II;
s2, carrying out gas-liquid separation on light oil gas in the oil gas to be recovered and oil gas from the top of the absorption tower in the liquid separation tank II, and sequentially conveying the separated oil gas to a condenser I and a condenser II for condensation treatment;
s3, conveying the non-condensable oil gas condensed in the step S2 to a liquid separating tank IV for gas-liquid separation, reheating the separated oil gas, conveying the reheated oil gas to an adsorption tank for adsorption treatment, and discharging the adsorbed tail gas up to the standard.
The oil gas to be recovered is divided into light oil gas and heavy oil gas according to the physical properties of the components, and the light oil gas and the heavy oil gas are separately recovered; if the recovered oil gas is light oil gas, the steps S2-S3 are performed, and if the recovered oil gas is heavy oil gas or light-heavy oil gas mixture, the steps S1-S3 are required.
The heavy oil gas refers to hydrocarbon mixture steam with the freezing point of 90 ℃ or above, such as wax oil and the like;
the light oil gas refers to hydrocarbon mixture steam or non-condensable gas with freezing point below 90 ℃, such as light oil and the like.
When the method is used for recovering the easily condensable oil gas, the heat tracing treatment can be started on the liquid separation tank I during the operation in winter, and the pipeline for conveying the easily condensable oil gas also needs to be subjected to heat tracing treatment.
In the above method, in step S1, a blower is used to convey the heavy oil gas to the absorption tower;
preferably, a variable frequency motor is adopted, the blower is interlocked with the pressure of the liquid separation tank I, and the blower is interlocked and stopped when the pressure is less than a set value (preferably set to be 0.5 KPaG); when the pressure is higher than the set value by 0.05KPaG (preferably 0.55KPaG), the blower is manually started, the frequency of the blower motor is adjusted along with the increase of the inlet pressure, the pressure of the liquid separation tank I is maintained to be 0.55KPaG, and the outlet pressure of the blower is maintained to be 34 KPaG.
In the above method, before being sent to the absorption tower in step S1, the method further includes a step of boosting the pressure of the oil gas;
in the step S2, before the oil gas is conveyed to the condenser I, the method further comprises the step of boosting the pressure of the oil gas, before the pressure boosting is carried out, the oxygen content in the oil gas needs to be analyzed through an online analysis instrument, if the oxygen content is qualified, the pressure boosting is carried out, otherwise, a torch is directly discharged, and the online analysis instrument is interlocked with a compressor outlet pipeline switch valve for boosting;
the pressure is increased by a blower or a compressor.
In the above method, in step S1, the absorption column is a packed column or a plate column;
preferably, a two-section packed tower is adopted, and middle-section reflux is adopted to improve the absorption efficiency of the absorbent;
the operating pressure of the absorption tower is 5 KPaG-15 KPaG, and micro-positive pressure is kept;
the absorbent is diesel oil or naphtha.
In the above method, in step S1, the absorbent is discharged from the bottom of the absorption tower, and is conveyed to a slop tank after flowing through a heat exchanger, or a part of the absorbent is conveyed to the middle part of the absorption tower to be refluxed at the middle part, and is used as a circulating absorbent, and the remaining absorbent is conveyed to the slop tank, and the proportion of the circulating part can be 0.5, or any proportion in the range of 0 to 1, and the proportion can be adjusted on site according to the actual absorption condition. .
In the above method, in step S2, before the oil gas is sent to the condenser i, the method further includes a step of performing oil gas separation on the oil gas in a liquid separation tank III, and performing gas-liquid separation through the liquid separation tank ii to prevent the oil-gas entrained liquid from damaging the compressor; and gas-liquid separation is carried out through the liquid separation tank III so as to prevent oil gas from carrying liquid to block the condenser or enhance the heat exchange effect.
In the method, in the step S2, the oil gas is condensed to 20-50 ℃ through the condenser I, and then is condensed to 0-10 ℃ through the condenser II;
and the refrigerants adopted by the condenser I and the condenser II are propylene or liquid ammonia.
In the above method, in step S3, the adsorbent is granular activated carbon or activated carbon fiber;
in step S3, the two adsorption tanks are alternately used for adsorption treatment and desorption treatment;
the desorption treatment adopts a vacuum desorption or high-temperature desorption method;
when vacuum desorption is adopted, the pumped tail gas is conveyed to the liquid separation tank II, then hot nitrogen is introduced into the adsorption tank for regeneration, and the regenerated tail gas is conveyed into a torch system.
When the activated carbon is used as an adsorbent, the temperature of the adsorption tank is controlled not to exceed a set value (80 ℃) during adsorption treatment, the pressure of the adsorption tank is made to be as low as possible (1PaA) when vacuum pumping is used, the adsorption efficiency and the regeneration efficiency are improved, the switching between the adsorption tank and the desorption tank is controlled sequentially, and the switching period is 2 hours.
The oil gas is discharged up to the standard through three-stage process treatment of absorption, condensation and adsorption, the oil gas treatment efficiency is improved through separate collection of light oil gas and heavy oil gas, the temperature of the heavy oil gas is high and the heavy oil gas is easy to condense, so that the heavy component in the heavy oil gas is treated independently by using an absorbent in an absorption part, and the fully absorbed heavy oil gas enters a subsequent process for continuous treatment; and the light oil gas is condensed and then is recycled to be partially oil product, finally is discharged after reaching the standard through the adsorption part, and if the light oil gas is not up to the standard in the accident state, the light oil gas can be discharged to a torch in an interlocking control mode, so that the direct discharge of the light oil gas into the atmosphere is avoided.
The method of the invention has the following characteristics:
(i) the invention provides a novel oil gas recovery method, which can improve the recovery efficiency of the whole process flow while ensuring that the oil gas emission reaches the standard;
(ii) the combined scheme of absorption, condensation and adsorption is adopted to separately recover and treat the light oil gas and the heavy oil gas, so that the recovered oil gas is treated more fully, and the oil gas recovery efficiency is improved;
(iii) the existing conditions of project construction sites are utilized to the maximum extent for oil gas recovery, and the coal chemical project can utilize the propylene washed by low-temperature methanol as a refrigerant of a condensation process, so that the energy consumption is reduced, and the investment is reduced;
(iv) when vacuum desorption is adopted, tail gas pumped out by a vacuum pump returns to the front end of the condensation process, so that the concentration of oil gas is increased to facilitate condensation;
(v) the desorption of the adsorption tank adopts vacuum and hot nitrogen combined desorption regeneration, so that the desorption regeneration effect is improved, the adsorption effect is ensured, and the oil gas emission reaches the standard;
(vi) the treated oil gas can be directly discharged to atmosphere when meeting the discharge standard, and can be discharged to a torch system if the accident does not meet the standard, so that the environmental pollution is avoided.
Drawings
FIG. 1 is a schematic view of a first process flow of the process of the present invention.
FIG. 2 is a schematic view of a second process flow of the method of the present invention.
FIG. 3 is a schematic process flow diagram of comparative example 1 in an embodiment of the present invention.
FIG. 4 is a schematic process flow diagram of comparative example 2 in an embodiment of the present invention.
The respective symbols in the figure are as follows:
1. a liquid separation tank I; 2. a blower; 3. a centrifugal pump I; 4. an absorption tower; 5. a centrifugal pump II; 6. a heat exchanger I; 7. a liquid separation tank II; 8. a compressor; 9. a liquid separating tank III; 10. a condenser I; 11. a condenser II; 12. a liquid separation tank IV; 13. an adsorption tank I; 14. an adsorption tank II; 15. a vacuum pump; 16. and a heat exchanger II.
Detailed Description
The experimental procedures used in the following examples are all conventional procedures unless otherwise specified.
Materials, reagents and the like used in the following examples are commercially available unless otherwise specified.
The invention provides a method for recovering and treating mixed oil gas containing light and heavy components, which comprises the following steps:
(1) the oil gas to be recovered is divided into light oil gas and heavy oil gas according to the physical properties of the components, and the light oil gas and the heavy oil gas are separated for recovery treatment;
(2) sending heavy oil gas into a liquid separation tank I for gas-liquid separation, and then boosting the pressure of the heavy oil gas through a blower;
(3) and (3) sending the heavy oil gas after pressure boosting into an absorption tower for absorption, and conveying an absorbent to the top of the absorption tower downwards through a centrifugal pump I to perform reverse absorption with the oil gas upwards from the bottom of the absorption tower. Oil gas from the top of the absorption tower enters a liquid separation tank II;
(4) the absorbent at the bottom of the absorption tower is sent to the middle part of the absorption tower through a centrifugal pump II and a heat exchanger I for middle-section reflux to be used as a circulating absorbent, and the other part of the absorbent is sent to a sump oil tank;
(5) sending the light oil gas into a liquid separation tank II, carrying out gas-liquid separation on the light oil gas, the oil gas at the top of the absorption tower and the tail gas after vacuum desorption, and then entering a compressor for boosting pressure;
(6) the oil gas after being boosted is sent into a liquid separation tank III, and then the oil gas respectively enters a condenser I and a condenser II for condensation treatment;
(7) sending the condensed non-condensable oil gas into a liquid separation tank IV for gas-liquid separation, then sending the oil gas into an adsorption tank for adsorption treatment, and discharging the tail gas after adsorption up to the standard;
(8) and the two adsorption tanks are alternately subjected to adsorption/desorption treatment, during the desorption treatment, the activated carbon is regenerated by vacuumizing through a vacuum pump, the pumped tail gas is sent to the liquid separation tank II, then hot nitrogen is introduced into the adsorption tanks for continuous regeneration, and the regenerated tail gas is sent to a torch system.
Preferably, in the step (1), the easily condensable oil gas is recycled, heat tracing treatment can be started for the branch tank I during winter operation, and a pipeline for conveying the easily condensable oil gas also needs heat tracing treatment.
Preferably, in the step (2), the blower uses a variable frequency motor, the blower is interlocked with the pressure of the liquid separation tank 1, and the blower is interlocked and stopped when the pressure is less than a set value (preferably set to be 0.5 KPaG); when the pressure is higher than the set value by 0.05KPaG (preferably 0.55KPaG), the blower is manually started, the frequency of the blower motor is adjusted along with the rise of the inlet pressure, and the pressure of the liquid separation tank 1 is maintained at 0.55 KPaG. The blower outlet pressure 34 KPaG.
Preferably, in the step (3), the absorption tower is a two-section packed tower, and middle-section reflux is used for improving the absorption efficiency of the absorbent. The operation pressure of the absorption tower is 5 KPaG-15 KPaG, and the micro-positive pressure is kept.
Preferably, in step (4), 50% of the absorbent at the bottom of the absorption column is refluxed as a circulating absorbent in the middle stage, and the other 50% is sent to a slop tank, and the ratio can be adjusted on site according to the actual absorption condition.
Preferably, in the step (5), the oxygen content in the oil gas is analyzed by an online analysis instrument before the oil gas enters the compressor for boosting, if the oxygen content is qualified, the oil gas is sent to the compressor for boosting, otherwise, a torch is directly discharged, and the online analysis instrument is interlocked with a switch valve of an outlet pipeline of the compressor.
Preferably, in the step (6), the oil gas is condensed to 35 ℃ after passing through the condenser 1, and then condensed to 5 ℃ through the condenser 2. The oil gas condensed by the condenser 2 can be used as a cold source of the condenser 1 to improve the utilization efficiency of cold energy, and the temperature of the uncondensed oil gas entering the adsorption tank is 17 ℃.
Preferably, in the step (7), activated carbon is used as the adsorbent, the temperature rise of the adsorption tank should be controlled not to exceed a set value (80 ℃) during adsorption treatment, the pressure of the adsorption tank should be reduced as much as possible (1PaA) during vacuum pumping by using a vacuum pump, the adsorption efficiency and the regeneration efficiency are improved, the switching between the adsorption tank and the desorption tank is controlled sequentially, and the switching period is 2 hours.
Preferably, in the step (8), the desorption method selects vacuum and hot nitrogen combination for desorption, the vacuum desorption tail gas is sent to the condensation front end, and the hot nitrogen desorption tail gas is discharged to a torch system.
The oil gas recovery treatment is carried out according to the method, so that the concentration of non-methane total hydrocarbons is effectively reduced, the standard requirement of emission of atmosphere is met, and the oil gas recovery efficiency is improved.
Examples 1,
In this embodiment, oil gas of 120 ten thousand tons/year fine chemical demonstration project of the hang brocade flag in the middle tank area of the light sump oil tank, the heavy sump oil tank, the wax tank and the synthetic water tank is used as oil gas to be recovered, wherein the oil gas process parameters of the wax tank are as follows: the operation temperature is 120 ℃, and the operation pressure is 0.8 KPaG; the oil gas technological parameters of other tanks are as follows: the operating temperature was 40 ℃ and the operating pressure was 1 KPaG.
The heavy oil gas components and the light oil gas components in this example are shown in tables 1 and 2.
As shown in fig. 1, the present embodiment performs oil and gas recovery by the following method, which specifically includes the following steps:
(1) oil gas in a wax tank in oil gas to be recovered is independently collected and recovered as heavy oil gas, and oil gas in other tanks is recovered as light oil gas;
(2) oil gas in a wax tank is sent into a liquid separation tank I1 for gas-liquid separation, and then the pressure of the wax oil gas is raised to 34KPaG through a blower 2;
(3) sending the pressurized wax oil gas into an absorption tower 4 for absorption, wherein the absorption tower 4 adopts a two-section type packed tower, and the process parameters of the absorption tower are as follows: the operation temperature of the top of the tower is 40 ℃, the operation pressure is 5KPaG, the operation temperature of the bottom of the tower is 70 ℃, and the operation pressure is 15 KPaG. The wax oil gas enters from the bottom of the tower and is absorbed upwards in the reverse direction with the absorbent, and the absorbed tower top oil gas is sent to a liquid separation tank II 7. The existing refined common second-line diesel oil in the absorbent selection project has the flow rate of 2000Kg/h, and is conveyed to the top of the absorption tower downwards through a centrifugal pump I3 to perform reverse absorption with oil gas from the bottom of the absorption tower upwards.
(4) After the tower bottom absorbent is cooled by a centrifugal pump II 5 and a heat exchanger I6 (the temperature is 40 ℃, the pressure is 500KPaG), 50 percent of the tower bottom absorbent is sent to the middle part of the absorption tower 4 for middle-section reflux to be used as a circulating absorbent, and the rest 50 percent of the tower bottom absorbent is sent to a sump oil tank;
(5) sending the light oil gas into a liquid separation tank II 7, carrying out gas-liquid separation together with oil gas at the top of the absorption tower and tail gas after vacuum desorption, and then entering a compressor 8 to increase the pressure to 304 KPaG;
(6) and (3) sending the oil gas after pressure boosting into a liquid separation tank III 9, and then sending the oil gas into a condenser I10 and a condenser II 11 for precooling and quenching in sequence. The process conditions of the precooling treatment of the condenser I10 are as follows: tube pass inlet and outlet temperature 40/35 ℃, inlet and outlet pressure 264/254 KPaG: the temperature of the inlet and outlet of the shell pass is 5/17 ℃, and the pressure of the inlet and outlet is 244/234 KPaG. The process conditions of the quenching treatment of the condenser II 11 are as follows: the inlet and outlet temperature of the tube pass is 35/5 ℃, and the inlet and outlet pressure is 254/244 KPaG; the inlet and outlet temperature of the shell pass is-17/-3 ℃, and the inlet and outlet pressure is 255/255 KPaG. The tube side of the condenser II 11 passes through oil gas, the shell side passes through a refrigerant propylene, and the propylene comes from a low-temperature methanol washing unit existing in the project. After gas-liquid separation of the oil gas subjected to quenching treatment in a liquid separation tank IV 12, the oil gas is used as a cold source of a condenser I10 and passes through the shell pass of the condenser I10, and the oil gas to be condensed passes through the tube pass of the condenser I10;
(7) the uncondensed oil gas (the temperature is 17 ℃, and the pressure is 234KPaG) passing through the condenser I10 enters an adsorption tank for adsorption treatment, the adsorption tank is subjected to adsorption/desorption treatment alternately through sequential control, and the switching period is 2 h. The process conditions of the adsorption treatment are as follows: the temperature is not more than 80 ℃; during adsorption treatment, oil gas enters from the bottom of the adsorption tank and upwards contacts with the activated carbon in an adsorption manner, and is discharged from the top of the adsorption tank. The tail gas discharged from the top of the adsorption tank meets the specification requirement and then is discharged into the atmosphere, and if the tail gas does not meet the specification requirement, the tail gas is sent to a torch;
(8) the process conditions of the desorption treatment are as follows: the operating pressure was 1 KPaA. During desorption treatment, the activated carbon is regenerated by vacuumizing through a vacuum pump, the extracted tail gas is sent to the liquid separation tank 2, after vacuum desorption, hot nitrogen is introduced for continuous regeneration, and the regenerated tail gas is sent to a torch system.
Examples 2,
As shown in fig. 1, this embodiment generally adopts the technical solution of embodiment 1, and the difference is that in the absorption process of this embodiment, naphtha is used as an absorbent, liquid ammonia is used as a refrigerant in the condensation process, and activated carbon fiber is used as an adsorbent in the adsorption process. All steps in the implementation were in accordance with example 1.
Examples 3,
As shown in fig. 2, this embodiment generally adopts the technical solution of embodiment 1, except that this embodiment does not include steps (1) to (4), i.e., has no absorption portion.
In the embodiment, the light oil gas is used as the oil gas to be recovered, the condensing and adsorbing processes are included, in the step (5), the light oil gas is sent to the liquid separation tank II 7 for gas-liquid separation, and enters the compressor 8 together with the tail gas after desorption and regeneration to be pressurized to 304 KPaG; steps (6) to (8) correspond to example 1.
Comparative examples 1,
As shown in fig. 3, the present comparative example generally adopts the technical solution of example 1, except that the light and heavy oil-gas mixture of the present comparative example is not separately treated and does not include steps (1) to (4), i.e., there is no absorption portion.
The comparative example uses the light and heavy mixed oil gas as the oil gas to be recovered, and comprises condensation and adsorption processes, wherein the light and heavy mixed oil gas is sent to the liquid separation tank II 7 in the step (5) for gas-liquid separation, and the subsequent steps are consistent with those in the example 3.
Comparative examples 2,
As shown in fig. 4, this comparative example generally adopts the technical solution of example 1, except that the light and heavy mixed oil gas of this comparative example is not separately treated and does not include step (6), i.e., there is no condensing part.
The comparative example uses the light and heavy mixed oil gas as the oil gas to be recovered, comprises the absorption and adsorption processes, the oil gas boosted by the compressor 8 in the step (7) directly enters the adsorption tank for adsorption treatment, and the subsequent steps are consistent with those in the example 1.
TABLE 1 heavy oil gas composition
TABLE 2 light oil gas composition
| Components | Molecular weight | Mole percent (mol%) |
| Nitrogen gas | 28 | 0.588 |
| Steam of water | 18 | 0.09 |
| Butene (butylene) | 56 | 0.12 |
| Butane | 58 | 0.1 |
| N-pentane | 72 | 0.05 |
| Hexene | 84 | 0.05 |
| C6+ | 0.002 | |
| Total of | 1 |
Table 3 total hydrocarbon content and removal efficiency of non-methane in exhaust gas of examples 1 to 3 and comparative examples 1 to 2
As can be seen from the table, the content of non-methane total hydrocarbons in the exhaust tail gas obtained by the method is 100-110 mg/Nm3And the removal efficiency is more than 97 percent, and the emission requirement of non-methane total hydrocarbons is met.
Claims (10)
1. A method of oil and gas recovery, comprising the following steps S1-S3 or S2-S3:
s1, conveying heavy oil gas in oil gas to be recovered to a liquid separating tank I for gas-liquid separation, conveying the oil gas obtained by separation to an absorption tower from the bottom of the absorption tower, reversely absorbing the oil gas with an absorbent from the top of the absorption tower, discharging the oil gas from the top of the absorption tower, and then feeding the oil gas into a liquid separating tank II;
s2, carrying out gas-liquid separation on light oil gas in the oil gas to be recovered and oil gas from the top of the absorption tower in the liquid separation tank II, and sequentially conveying the separated oil gas to a condenser I and a condenser II for condensation treatment;
s3, conveying the non-condensable oil gas condensed in the step S2 to a liquid separating tank IV for gas-liquid separation, conveying the separated oil gas after reheating to an adsorption tank for adsorption treatment, and discharging the adsorbed tail gas after reaching the standard.
2. The method of claim 1, wherein: the heavy oil gas refers to hydrocarbon mixture steam with the freezing point of 90 ℃ and above;
the light oil gas refers to hydrocarbon mixture steam or non-condensable gas with the freezing point below 90 ℃.
3. The method according to claim 1 or 2, characterized in that: in step S1, before being conveyed to the absorption tower, the method further comprises the step of boosting the pressure of the oil gas;
in step S2, before being conveyed to the condenser I, the method further comprises the step of boosting the pressure of the oil gas;
the pressure is increased by a blower or a compressor.
4. The method according to any one of claims 1-3, wherein: in step S1, the absorption tower is a packed tower or a plate tower;
the absorbent is diesel oil or naphtha.
5. The method according to any one of claims 1-4, wherein: in step S1, the absorbent is discharged from the bottom of the absorption tower, flows through a heat exchanger and is then transported to a slop tank, or a part of the absorbent is transported to the middle of the absorption tower to undergo middle-stage reflux, and is used as a circulating absorbent, and the remaining amount of the absorbent is transported to the slop tank.
6. The method according to any one of claims 1-5, wherein: in the step S2, the oil gas is condensed to 20-50 ℃ through the condenser I, and then condensed to 0-10 ℃ through the condenser II;
and the refrigerants adopted by the condenser I and the condenser II are propylene or liquid ammonia.
7. The method according to any one of claims 1-6, wherein: in step S3, the adsorbent is granular activated carbon or activated carbon fiber.
8. The method according to any one of claims 1-7, wherein: in step S3, the two adsorption tanks are alternately used to perform adsorption treatment and desorption treatment.
9. The method of claim 8, wherein: the desorption treatment adopts a vacuum desorption or high-temperature desorption method;
when vacuum desorption is adopted, the pumped tail gas is conveyed to the liquid separation tank II, then hot nitrogen is introduced into the adsorption tank for regeneration, and the regenerated tail gas is conveyed into a torch system.
10. The method according to any one of claims 1-9, wherein: in step S2, before the oil gas is conveyed to the condenser I, the method further comprises the step of carrying out oil gas separation on the oil gas in a liquid separation tank III.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113786700A (en) * | 2021-09-01 | 2021-12-14 | 广东申菱环境系统股份有限公司 | Oil gas recovery system |
| CN114053842A (en) * | 2021-10-29 | 2022-02-18 | 青岛诺诚化学品安全科技有限公司 | Recovery system and method for dissipated flue gas in liquid asphalt loading process |
| CN114317038A (en) * | 2021-12-29 | 2022-04-12 | 山东宝塔新能源有限公司 | Coal tar recovery and collection device |
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| CN108689381A (en) * | 2018-06-26 | 2018-10-23 | 武汉轻工大学 | A kind of area of refinery oil loading platform gas recovery system for oil and its recovery method |
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