CN113018891B - Method for carrying out step-by-step condensation on oil gas recovery by utilizing LNG cold energy - Google Patents
Method for carrying out step-by-step condensation on oil gas recovery by utilizing LNG cold energy Download PDFInfo
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
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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
- C10G5/02—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with solid 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
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
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Abstract
The invention relates to a method for carrying out gradual condensation on oil gas recovery by utilizing LNG cold energy, which belongs to the technical field of chemical industry and environmental protection, and adopts a condensation and refueling gas capture integrated process, comprising feed gas separation, first-stage separation, second-stage separation, third-stage separation, gas doping, fourth-stage separation, gas adsorption and light hydrocarbon storage, and the method has the advantages that: the gas after adsorption can reach the direct discharge standard of VOC; the cold energy required by the oil gas recovery completely comes from the cold energy released by the LNG gasification, and is stable and low in energy consumption; further improves the removal rate of final organic matters, and can improve the removal rate to 99.58-99.74% and the like.
Description
Technical Field
The invention relates to the technical field of chemical engineering and environmental protection, in particular to a method for recycling oil gas by using LNG cold energy to carry out stepwise condensation.
Background
The existing oil gas recovery process technology mainly comprises an RTO waste gas treatment process and a catalytic combustion oil gas treatment process.
The RTO waste gas treatment process specifically comprises the steps of feeding organic waste gas into a regenerative chamber (RTO) through a blower to preheat to about 750 ℃, then feeding the organic waste gas into a thermal oxidation chamber to be fully oxidized and decomposed, enabling the temperature of the thermal oxidation chamber to reach 800-850 ℃ under the action of combustion-supporting fuel, enabling organic components in the waste gas to be fully oxidized and decomposed, enabling generated flue gas to enter another group of regenerative chambers to exchange heat with thermal storage ceramic fillers, discharging the heat-exchanged flue gas through a chimney, continuously and circularly regenerating the process, and alternately switching each regenerative chamber between modes of inputting the waste gas and discharging the treated gas.
However, the RTO exhaust gas treatment process has the following disadvantages: in the prior art, the RTO waste gas combustion process has high combustion temperature and harsh operating conditions; the RTO waste gas combustion technology in the prior art has high energy consumption; the CO2 generated by the RTO waste gas combustion process is partially inconsistent with the carbon reaching standard idea proposed by the nation, and the greenhouse effect is increased.
The specific operation of the catalytic combustion waste gas treatment process is that the concentration of organic waste gas is concentrated by 10-20 times by controlling the flow rate in the desorption process, then the desorbed gas flow is heated to about 300 ℃ by an electric heating device arranged in a catalytic bed, the desorbed gas flow is combusted under the action of a catalyst, CO2 and H2O are generated after the combustion and release a large amount of heat, the heat is used for heating the desorbed high-concentration waste gas through a heat exchanger part in the catalytic combustion bed, the air outside the other part of the heating chamber is used as the activated carbon desorbed gas, the electric heater is generally started for about 1 hour when the self-balancing process of desorption-catalytic combustion is achieved, the electric heating device can be closed after the heat balance is achieved, and the regeneration treatment system depends on the organic solvent in the waste gas as fuel.
However, the catalytic combustion waste gas treatment process has the following defects: the catalytic combustion oil gas recovery process is complex, the operation conditions are harsh, and the energy consumption is high under the operation working condition; the catalytic combustion oil gas recovery process needs to be in contact with air to generate combustion reaction, so that potential safety hazards exist; the combustion products of the catalytic combustion oil gas recovery process, namely CO2 and H2O, are not in accordance with the carbon standard-reaching idea proposed by the country, and the intensification of the greenhouse effect is increased; the catalytic combustion investment cost is high; the reaction can be carried out only in the presence of a catalyst, so that hazardous waste of the catalyst can be generated, and the treatment cost is high.
The patent CN109163215A discloses an energy storage type oil gas recovery device and method for an oil gas combined station, which comprises a cold storage gas tank, a first compressor, a cold storage gas precooler, a fork-comb-tooth-shaped phase change cold storage device, an oil gas tank, a second compressor and a cold storage type oil gas precooler, wherein the fork-comb-tooth-shaped phase change cold storage device is provided with a fork-comb-tooth-shaped cold storage cavity, a circuitous mixed gas microchannel channel and a circuitous LNG microchannel channel with a porous material inserted therein; the recovery device can liquefy and settle the pressurized cold-storage gas in the fork-comb-tooth-shaped phase-change cold storage device after the pressurized cold-storage gas is efficiently absorbed in two stages, and the generated low-temperature CNG is further stored cold through the cold-storage type oil gas precooler; when the oil gas is recovered, the pressurized mixed gas is sequentially condensed by two-stage cold storage and high efficiency through a cold storage type oil gas precooler and a fork comb tooth type phase change cold storage device, and the oil gas is recovered. However, the recovery method needs to add power consumption equipment to further condense and cool the LNG, and the energy consumption is high.
Disclosure of Invention
In order to solve the technical problems in the prior art, the invention provides a method for recovering oil gas by using LNG cold energy to carry out stepwise condensation, so as to realize the following purposes:
the recovered uncondensed gas can reach the direct discharge standard of VOC, the cold energy required by oil gas recovery is completely from the cold energy released by LNG gasification, the method is stable and low in energy consumption, and the final organic matter removal rate can be improved to 99.58-99.74%.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows:
a method for recycling oil gas to be condensed step by utilizing LNG cold energy adopts a condensed refueling gas capture integrated process.
A method for carrying out gradual condensation on oil gas recovery by utilizing LNG cold energy comprises raw material gas separation, first-stage separation, second-stage separation, third-stage separation, gas doping, fourth-stage separation, gas adsorption and light hydrocarbon storage.
And separating the raw material gas, namely, after the raw material gas enters a boundary region, firstly, entering a raw material gas buffer tank to separate a liquid component to obtain a gas-phase component, boosting the gas-phase component to 80KPa by a Roots blower, raising the temperature to 85-88 ℃, and then re-heating to 55-58 ℃ to obtain a re-heated gas-phase component.
And in the first-stage separation, the gas-phase component after rewarming is introduced into a first-stage cooler to be cooled to 4 ℃, and the gas-phase component after cooling enters a first-stage separator to separate a first-stage liquid component.
And the flow rate of the gas-phase components after being reheated when the gas-phase components are introduced into the first-stage cooler is 40-50L/min.
The cold energy of the primary cooler is from tail gas after low-temperature separation and partially gasified BOG gas.
The first-stage liquid phase component is water.
And in the second-stage separation, the gas phase separated by the first-stage separator is introduced into a second-stage cooler to be cooled to-40 ℃, and then enters a second-stage separator to separate a second-stage liquid component.
The secondary liquid component is a hydrocarbon-water mixture.
And two coolers are arranged for cooling in the secondary separation process, wherein when one cooler is used for cooling, the other cooler is cooled to minus 40 ℃ again after the temperature is increased to 10 ℃, and the switching is carried out every 30min on average.
And in the third-stage separation, the gas phase separated by the second-stage separator is introduced into a third-stage cooler to be cooled to-80 ℃, and then enters the third-stage separator to separate a third-stage liquid component.
The three-stage liquid component is a hydrocarbon-water mixture.
And doping the gas, namely adding doping gas into the gas phase separated by the three-stage separator to obtain the doped gas phase.
Wherein the volume ratio of the gas phase separated by the three-stage separator to the doping gas is 7-8: 1.
The doping gas is a mixture of ethane, nitrogen and oxygen, wherein the volume ratio of the ethane, the nitrogen and the oxygen is 4-5:12-15: 1.
And the fourth-stage separation is to cool the doped gas phase to-115 to-120 ℃ in a fourth-stage cooler and then enter a fourth-stage separator to separate out a fourth-stage liquid component.
The components of the four-stage liquid component are C5 and hydrocarbons with more than C5.
And the gas adsorption is to compress and exchange heat of the gas passing through the four-stage separator by a Roots blower, then enter a downstream oil gas adsorption tower, and directly discharge the gas into the air after adsorption is completed.
The control pressure in the compression heat exchange of the Roots blower is 50MPa, and the temperature is 55 ℃.
The adsorption medium of the downstream oil gas adsorption tower is activated carbon, diatomite and puffed soybean meal, wherein the mass ratio of the activated carbon to the diatomite to the puffed soybean meal is 20-23: 16-18: 2-4.
The particle size of the diatomite is 70-100 mu m.
The particle size of the puffed soybean powder is 500-550 mu m.
The adsorption temperature of the downstream oil gas adsorption tower is 50 ℃, and the pressure is 10 MPa.
The LNG cold energy is sent to the four-stage cooler, the three-stage cooler and the two-stage cooler in sequence after flowing out of the storage tank to provide sufficient cold energy for oil gas cooling.
And the light hydrocarbon is stored, the hydrocarbon mixture separated from the raw gas by the second-stage, third-stage and fourth-stage separators is introduced into a light hydrocarbon buffer tank for storage, and the water separated by the first-stage separator is connected to a specified position.
The pressure of the light hydrocarbon buffer tank is 0.15MPa, and the temperature is 25-30 ℃.
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the method for recycling the oil gas by utilizing the LNG cold energy, the gas after adsorption is enabled to reach the direct discharge standard of VOC through four-stage condensation separation;
(2) according to the method for gradually condensing the oil gas recovery by using the LNG cold energy, the cold energy required by the oil gas recovery completely comes from the cold energy released by the LNG gasification, and is stable and low in energy consumption;
(3) according to the method for carrying out gradual condensation on oil gas recovery by utilizing LNG cold energy, through gas doping and further adsorption by using activated carbon, diatomite and expanded soybean meal, the volume fraction of methane in the gas after adsorption is finished can be reduced to 0-0.01%, the volume fraction of ethane can be reduced to 0-0.02%, the volume fraction of propane can be reduced to 0%, the volume fraction of isobutane can be reduced to 0-0.02%, the volume fraction of n-butane can be reduced to 0-0.02%, the volume fraction of isopentane can be reduced to 0-0.01%, the volume fraction of n-pentane can be reduced to 0-0.01%, and the volume fraction of hydrocarbons above C5 can be reduced to 0.01-0.03%;
(4) the method for recovering the oil gas by using the LNG cold energy to condense step by step further improves the removal rate of final organic matters by doping gas and further adsorbing by using the activated carbon, the diatomite and the puffed soybean meal, and can improve the removal rate to 99.58-99.74 percent.
Detailed Description
In order to more clearly understand the technical features, objects, and effects of the present invention, specific embodiments of the present invention will now be described.
Example 1
A method for recycling oil gas to be condensed step by utilizing LNG cold energy adopts a condensed refueling gas capture integrated process.
A method for carrying out gradual condensation on oil gas recovery by utilizing LNG cold energy comprises raw material gas separation, first-stage separation, second-stage separation, third-stage separation, gas doping, fourth-stage separation, gas adsorption and light hydrocarbon storage.
After the raw material gas enters the boundary region, the raw material gas firstly enters a raw material gas buffer tank to separate liquid components to obtain gas-phase components, the gas-phase components are pressurized to 80KPa by a Roots blower, the temperature is raised to 85 ℃, and then the gas-phase components are reheated to 55 ℃ to obtain reheated gas-phase components.
And in the first-stage separation, the gas-phase component after rewarming is introduced into a first-stage cooler to be cooled to 4 ℃, and the gas-phase component after cooling enters a first-stage separator to separate a first-stage liquid component.
The flow rate of the gas-phase components after rewarming when the gas-phase components are introduced into the first-stage cooler is 40L/min.
The cold energy of the primary cooler is from tail gas after low-temperature separation and partially gasified BOG gas.
The first-stage liquid phase component is water.
And in the second-stage separation, the gas phase separated by the first-stage separator is introduced into a second-stage cooler to be cooled to-40 ℃, and then enters a second-stage separator to separate a second-stage liquid component.
The secondary liquid component is a hydrocarbon-water mixture.
And two coolers are arranged for cooling in the secondary separation process, wherein when one cooler is used for cooling, the other cooler is cooled to minus 40 ℃ again after the temperature is increased to 10 ℃, and the switching is carried out every 30min on average.
And in the third-stage separation, the gas phase separated by the second-stage separator is introduced into a third-stage cooler to be cooled to-80 ℃, and then enters the third-stage separator to separate a third-stage liquid component.
The three-stage liquid component is a hydrocarbon-water mixture.
And doping the gas, namely adding doping gas into the gas phase separated by the three-stage separator to obtain the doped gas phase.
Wherein the volume ratio of the gas phase separated by the three-stage separator to the doping gas is 7-8: 1.
The doping gas is a mixture of ethane, nitrogen and oxygen, wherein the volume ratio of the ethane, the nitrogen and the oxygen is 4:12: 1.
And the fourth-stage separation is to enter the doped gas phase into a fourth-stage cooler to be cooled to-115 ℃, and then enter a fourth-stage separator to separate out a fourth-stage liquid component.
The components of the four-stage liquid component are C5 and hydrocarbons with more than C5.
And the gas adsorption is to compress and exchange heat of the gas passing through the four-stage separator by a Roots blower, then enter a downstream oil gas adsorption tower, and directly discharge the gas into the air after adsorption is completed.
The control pressure in the compression heat exchange of the Roots blower is 50MPa, and the temperature is 55 ℃.
The adsorption medium of the downstream oil gas adsorption tower is activated carbon, diatomite and expanded soybean meal, wherein the mass ratio of the activated carbon to the diatomite to the expanded soybean meal is 20:16: 2.
The particle size of the diatomite is 70 μm.
The particle size of the puffed soybean powder is 500 mu m.
The adsorption temperature of the downstream oil gas adsorption tower is 50 ℃, and the pressure is 10 MPa.
The LNG cold energy is sent to the four-stage cooler, the three-stage cooler and the two-stage cooler in sequence after flowing out of the storage tank to provide sufficient cold energy for oil gas cooling.
The hydrocarbon mixture separated from the raw gas by the second, third and fourth separators is introduced into a light hydrocarbon buffer tank for storage, and the water separated by the first separator is connected to a designated position.
The pressure of the light hydrocarbon buffer tank is 0.15MPa, and the temperature is 25 ℃.
Example 2
A method for recycling oil gas to be condensed step by utilizing LNG cold energy adopts a condensed refueling gas capture integrated process.
A method for carrying out gradual condensation on oil gas recovery by utilizing LNG cold energy comprises raw material gas separation, first-stage separation, second-stage separation, third-stage separation, gas doping, fourth-stage separation, gas adsorption and light hydrocarbon storage.
And separating the raw material gas, namely, after the raw material gas enters a boundary region, firstly, entering a raw material gas buffer tank to separate a liquid component to obtain a gas-phase component, boosting the gas-phase component to 80KPa by a Roots blower, raising the temperature to 85-88 ℃, and then re-heating to 55-58 ℃ to obtain a re-heated gas-phase component.
And in the first-stage separation, the gas-phase component after rewarming is introduced into a first-stage cooler to be cooled to 4 ℃, and the gas-phase component after cooling enters a first-stage separator to separate a first-stage liquid component.
And the flow rate of the gas-phase components after rewarming when the gas-phase components are introduced into the first-stage cooler is 45L/min.
The cold energy of the primary cooler is from tail gas after low-temperature separation and partially gasified BOG gas.
The first-stage liquid phase component is water.
And in the second-stage separation, the gas phase separated by the first-stage separator is introduced into a second-stage cooler to be cooled to-40 ℃, and then enters a second-stage separator to separate a second-stage liquid component.
The secondary liquid component is a hydrocarbon-water mixture.
And two coolers are arranged for cooling in the secondary separation process, wherein when one cooler is used for cooling, the other cooler is cooled to minus 40 ℃ again after the temperature is increased to 10 ℃, and the switching is carried out every 30min on average.
And in the third-stage separation, the gas phase separated by the second-stage separator is introduced into a third-stage cooler to be cooled to-80 ℃, and then enters the third-stage separator to separate a third-stage liquid component.
The three-stage liquid component is a hydrocarbon-water mixture.
And doping the gas, namely adding doping gas into the gas phase separated by the three-stage separator to obtain the doped gas phase.
Wherein the volume ratio of the gas phase separated by the three-stage separator to the doping gas is 7: 1.
The doping gas is a mixture of ethane, nitrogen and oxygen, wherein the volume ratio of the ethane, the nitrogen and the oxygen is 4:13: 1.
And the fourth-stage separation is to enter a fourth-stage cooler to cool the doped gas phase to-118 ℃, and then enter a fourth-stage separator to separate out a fourth-stage liquid component.
The components of the four-stage liquid component are C5 and hydrocarbons with more than C5.
And the gas adsorption is to compress and exchange heat of the gas passing through the four-stage separator by a Roots blower, then enter a downstream oil gas adsorption tower, and directly discharge the gas into the air after adsorption is completed.
The control pressure in the compression heat exchange of the Roots blower is 50MPa, and the temperature is 55 ℃.
The adsorption medium of the downstream oil gas adsorption tower is activated carbon, diatomite and expanded soybean meal, wherein the mass ratio of the activated carbon to the diatomite to the expanded soybean meal is 21:17: 3.
The particle size of the diatomite is 80 μm.
The particle size of the puffed soybean powder is 520 μm.
The adsorption temperature of the downstream oil gas adsorption tower is 50 ℃, and the pressure is 10 MPa.
The LNG cold energy is sent to the four-stage cooler, the three-stage cooler and the two-stage cooler in sequence after flowing out of the storage tank to provide sufficient cold energy for oil gas cooling.
And the light hydrocarbon is stored, the hydrocarbon mixture separated from the raw gas by the second-stage, third-stage and fourth-stage separators is introduced into a light hydrocarbon buffer tank for storage, and the water separated by the first-stage separator is connected to a specified position.
The pressure of the light hydrocarbon buffer tank is 0.15MPa, and the temperature is 28 ℃.
Example 3
A method for recycling oil gas to be condensed step by utilizing LNG cold energy adopts a condensed refueling gas capture integrated process.
A method for carrying out gradual condensation on oil gas recovery by utilizing LNG cold energy comprises raw material gas separation, first-stage separation, second-stage separation, third-stage separation, gas doping, fourth-stage separation, gas adsorption and light hydrocarbon storage.
And separating the raw material gas, namely, after the raw material gas enters a boundary region, firstly, entering a raw material gas buffer tank to separate a liquid component to obtain a gas-phase component, boosting the gas-phase component to 80KPa by a Roots blower, raising the temperature to 85-88 ℃, and then re-heating to 55-58 ℃ to obtain a re-heated gas-phase component.
And in the first-stage separation, the gas-phase component after rewarming is introduced into a first-stage cooler to be cooled to 4 ℃, and the gas-phase component after cooling enters a first-stage separator to separate a first-stage liquid component.
And the flow rate of the gas-phase components after rewarming when the gas-phase components are introduced into the first-stage cooler is 50L/min.
The cold energy of the primary cooler is from tail gas after low-temperature separation and partially gasified BOG gas.
The first-stage liquid phase component is water.
And in the second-stage separation, the gas phase separated by the first-stage separator is introduced into a second-stage cooler to be cooled to-40 ℃, and then enters a second-stage separator to separate a second-stage liquid component.
The secondary liquid component is a hydrocarbon-water mixture.
And two coolers are arranged for cooling in the secondary separation process, wherein when one cooler is used for cooling, the other cooler is cooled to minus 40 ℃ again after the temperature is increased to 10 ℃, and the switching is carried out every 30min on average.
And in the third-stage separation, the gas phase separated by the second-stage separator is introduced into a third-stage cooler to be cooled to-80 ℃, and then enters the third-stage separator to separate a third-stage liquid component.
The three-stage liquid component is a hydrocarbon-water mixture.
And doping the gas, namely adding doping gas into the gas phase separated by the three-stage separator to obtain the doped gas phase.
Wherein the volume ratio of the gas phase separated by the three-stage separator to the doping gas is 8: 1.
The doping gas is a mixture of ethane, nitrogen and oxygen, wherein the volume ratio of the ethane, the nitrogen and the oxygen is 5: 15: 1.
And the fourth-stage separation is to enter the doped gas phase into a fourth-stage cooler to be cooled to-120 ℃, and then enter a fourth-stage separator to separate out a fourth-stage liquid component.
The components of the four-stage liquid component are C5 and hydrocarbons with more than C5.
And the gas adsorption is to compress and exchange heat of the gas passing through the four-stage separator by a Roots blower, then enter a downstream oil gas adsorption tower to obtain the gas after adsorption is finished, and directly discharge the gas after adsorption into the air.
The control pressure in the compression heat exchange of the Roots blower is 50MPa, and the temperature is 55 ℃.
The adsorption medium of the downstream oil gas adsorption tower is activated carbon, diatomite and expanded soybean meal, wherein the mass ratio of the activated carbon to the diatomite to the expanded soybean meal is 23:18: 4.
The particle size of the diatomite is 100 mu m.
The particle size of the puffed soybean powder is 550 mu m.
The adsorption temperature of the downstream oil gas adsorption tower is 50 ℃, and the pressure is 10 MPa.
The LNG cold energy is sent to the four-stage cooler, the three-stage cooler and the two-stage cooler in sequence after flowing out of the storage tank to provide sufficient cold energy for oil gas cooling.
And the light hydrocarbon is stored, the hydrocarbon mixture separated from the raw gas by the second-stage, third-stage and fourth-stage separators is introduced into a light hydrocarbon buffer tank for storage, and the water separated by the first-stage separator is connected to a specified position.
The pressure of the light hydrocarbon buffer tank is 0.15MPa, and the temperature is 30 ℃.
Example 4
The method for gradually condensing oil gas recovery by using LNG cold energy described in embodiments 1-3 is adopted, and meanwhile, comparative tests 1-3 are set for comparison.
Comparative example 1: the method for gradually condensing oil gas recovery by using LNG cold energy in embodiment 1 is characterized in that: three separations were omitted.
Comparative example 2: the method for gradually condensing oil gas recovery by using LNG cold energy in embodiment 1 is characterized in that: gas doping is omitted.
Comparative example 3: the method for gradually condensing oil gas recovery by using LNG cold energy in embodiment 1 is characterized in that: expanded soybean meal was omitted from the gas adsorption.
The raw material gas before treatment comprises the following components in percentage by weight:
after the raw material gas is treated by the method for gradually condensing the oil gas recovery by using the LNG cold energy described in examples 1 to 3 and comparative examples 1 to 3, the residual hydrocarbons in the gas after the adsorption is completed are detected and the removal rate is calculated:
all percentages used in the present invention are mass percentages unless otherwise indicated.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The method for gradually condensing oil gas recovery by using LNG cold energy is characterized by comprising the following steps: the method adopts a condensing refueling gas capturing integrated process;
the method comprises the steps of raw material gas separation, first-stage separation, second-stage separation, third-stage separation, gas doping, fourth-stage separation, gas adsorption and light hydrocarbon storage;
the gas doping step is to add doping gas into the gas phase separated by the three-stage separator to obtain a doped gas phase;
wherein the volume ratio of the gas phase separated by the three-stage separator to the doping gas is 7-8: 1;
the doping gas is a mixture of ethane, nitrogen and oxygen, wherein the volume ratio of the ethane to the nitrogen to the oxygen is 4-5:12-15: 1;
the gas adsorption step is that the gas after passing through the four-stage separator is compressed and heat exchanged through a Roots blower, then enters a downstream oil gas adsorption tower, and is directly discharged into the air after adsorption is finished;
the control pressure in the compression heat exchange of the Roots blower is 50MPa, and the temperature is 55 ℃;
the adsorption medium of the downstream oil gas adsorption tower is activated carbon, diatomite and puffed soybean meal, wherein the mass ratio of the activated carbon to the diatomite to the puffed soybean meal is 20-23: 16-18: 2-4;
the particle size of the diatomite is 70-100 mu m;
the particle size of the puffed soybean powder is 500-550 mu m;
the adsorption temperature of the downstream oil gas adsorption tower is 50 ℃, and the pressure is 10 MPa.
2. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 1, characterized in that: and separating the raw material gas, namely, after the raw material gas enters a boundary region, firstly, entering a raw material gas buffer tank to separate a liquid component to obtain a gas-phase component, boosting the gas-phase component to 80KPa by a Roots blower, raising the temperature to 85-88 ℃, and then re-heating to 55-58 ℃ to obtain a re-heated gas-phase component.
3. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 1, characterized in that: and in the first-stage separation, the gas-phase component after rewarming is introduced into a first-stage cooler to be cooled to 4 ℃, and the gas-phase component after cooling enters a first-stage separator to separate a first-stage liquid component.
4. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 3, characterized in that: and the flow rate of the gas-phase components after being reheated when the gas-phase components are introduced into the first-stage cooler is 40-50L/min.
5. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 3, characterized in that: the cold energy of the primary cooler is from tail gas after low-temperature separation and partially gasified BOG gas.
6. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 1, characterized in that: and in the second-stage separation, the gas phase separated by the first-stage separator is introduced into a second-stage cooler to be cooled to-40 ℃, and then enters a second-stage separator to separate a second-stage liquid component.
7. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 6, characterized in that: and two coolers are arranged for cooling in the secondary separation process, wherein when one cooler is used for cooling, the other cooler is cooled to minus 40 ℃ again after the temperature is increased to 10 ℃, and the switching is carried out every 30min on average.
8. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 1, characterized in that: and in the third-stage separation, the gas phase separated by the second-stage separator is introduced into a third-stage cooler to be cooled to-80 ℃, and then enters the third-stage separator to separate a third-stage liquid component.
9. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 1, characterized in that: and the fourth-stage separation is to cool the doped gas phase to-115 to-120 ℃ in a fourth-stage cooler and then enter a fourth-stage separator to separate out a fourth-stage liquid component.
10. The method for progressive condensation of oil and gas recovery using LNG cold energy according to claim 1, characterized in that: and the LNG cold energy is sent to the four-stage cooler, the three-stage cooler and the two-stage cooler in sequence after flowing out of the storage tank to provide sufficient cold energy for oil gas cooling.
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