CN112745974B - Membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment - Google Patents
Membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
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Abstract
The invention discloses a membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment. Firstly, pressurizing low-pressure associated gas to a certain pressure by a compressor; secondly, the high-pressure associated gas enters an adsorption dehydration tower to remove water vapor, and the associated gas is used as regenerated gas in the adsorption process; and thirdly, allowing dry associated gas at the outlet of the dehydration tower to enter a throttling expansion unit, cooling by a throttling expansion valve, removing liquid hydrocarbon by a gas-liquid separator, exchanging heat between the low-temperature associated gas and the associated gas at the throttling expansion inlet to recover cold energy, and heating to 40-70 ℃ by a heater. Fourthly, the associated gas at the outlet of the heater enters a membrane separation unit, the associated gas is divided into two paths, and the membrane separation unit permeates residual gas (CO)2The content is less than or equal to 3 percent) is directly used as product gas to be transported or utilized by downstream pipelines, and the membrane separation permeation gas is rich in CO2And removing a torch or discharging the gas outside, and realizing the emission reduction and recycling of the associated gas.
Description
Technical Field
The invention belongs to the field of associated gas purification, and particularly relates to a membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment.
Background
Associated gas is gas generated along with petroleum liquid in the oil field during the exploitation process, the main component of the associated gas is methane, and the associated gas also contains macromolecular hydrocarbon components such as propane, butane and pentane, saturated steam and CO2And the like. They can be further processed to purify the recovered heavy hydrocarbon components and to remove water vapor, CO2And (4) after the components are mixed, the purified associated gas reaches the national natural gas pipeline transportation standard, and the heavy hydrocarbon component is recovered as liquefied natural gas. However, the gas quantity of associated gas is usually small and distributed scattered, the traditional absorption technology has large occupied area, high energy consumption and high requirements on a matching system and a field, and the adsorption method for recycling the small-sized associated gas is not economical economically. In addition, the associated gas is relatively difficult to control in the oilfield exploitation process, and the requirements on the operation elasticity and stability of equipment are high, so that a large part of the associated gas is emptied or burnt, on one hand, the resources are wasted, and on the other hand, the environmental pollution is caused.
The development of an associated gas purification process which is small in size, light in weight, low in energy consumption and flexible and variable in treatment scale is required. The membrane method gas separation technology is based on the speed difference of different gases penetrating through the membrane module, has no phase change in the process, has the advantages of low energy consumption, small occupied area, light weight, simple operation and maintenance, environmental friendliness and the like, can flexibly adjust the processing capacity according to the gas quantity, and is an ideal associated gas purification technology. There have been some reports on membrane separation associated gas purification, but due to improper design of pretreatment process, the performance of gas separation membrane is unstable, and improvement of pretreatment process is needed to keep membrane separation unit operating stably for a long time.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment, which are used for removing CO in associated gas2Water vapor, etc., to purify gasesAnd the recycling of associated gas is realized by the standard of natural gas pipeline transmission. And the processing capacity of the system can be flexibly adjusted according to the air source condition, so that the system can be kept to operate stably for a long time.
The invention provides a membrane separation method oilfield associated gas purification system based on adsorption dehydration pretreatment.
The gas compressor unit is used for pressurizing associated gas to a certain pressure, and the compressor unit can be a primary compressor unit, a secondary compressor unit or a tertiary compressor unit,
wherein each stage of compressor unit comprises a compressor, a cooler and a gas-liquid separator;
the pressure of the compressed associated gas compressed by the last stage compressor unit can be 7-10MPa, specifically 9MPa and 8.8MPa, the temperature can be 40-60 ℃, and specifically 45 ℃ or 40 ℃;
the compressed associated gas (namely the associated gas at the outlet of the compressor) compressed by the last stage of compressor unit enters an adsorption dehydration unit;
all liquid phase outlets of the gas-liquid separators of the compressor unit are connected with the discharge tank after being mixed;
the adsorption dehydration unit adopts an isobaric temperature swing adsorption process and consists of a dehydration tower, a regeneration gas heater, a regeneration gas cooler, a regeneration gas-liquid separator and a dust filter;
associated gas at the outlet of the compressor is firstly divided into two streams by an adjusting valve, one stream is about 10-25% used as regenerated gas, the regenerated gas returns to the inlet after the regeneration work is finished and is converged with the other stream of process gas about 75-90%, and the process gas enters a dehydration tower to finish purification.
Taking example 1 as an example: compressed associated gas accounting for 80% of the total amount is directly sent to a dehydration tower A through a program control valve, under the selective adsorption of an adsorbent bed layer in the dehydration tower, moisture in the gas is adsorbed, the gas which is not adsorbed is purified, and the gas enters a dust filter for dust removal through the program control valve; adsorbing and dehydrating the remaining 20% of associated gas by a dehydrating tower, heating the associated gas to 180 ℃ by a regeneration gas heater, desorbing the associated gas as an adsorbent in the dehydrating tower, cooling the regeneration gas rich in water vapor to 40-50 ℃ by a regeneration gas cooler, separating liquid water and gas in the gas from the regeneration gas cooler by a regeneration gas-liquid separator, returning the separated gas to an inlet to join with the main gas, and entering the dehydrating tower to complete purification;
when the front edge of the mass transfer zone (called adsorption front edge) of the adsorbed impurities reaches the reserved section of the bed outlet, the adsorption is stopped, the adsorption bed starts to shift to the regeneration process, and when the dehydration towers are in a purification state, the other two dehydration towers are in the regeneration process (one is in a hot blowing state, and the other is in a cold blowing state);
the gas content of associated gas at the outlet of the adsorption dehydration unit is reduced to 50 ppm;
the associated gas at the outlet of the adsorption dehydration unit enters a throttling expansion unit;
the throttling expansion unit comprises a gas heat exchanger, a throttling expansion valve, a gas-liquid separator, a coalescing filter and a heater;
the associated gas at the inlet of the throttling expansion unit is subjected to heat exchange, temperature reduction, heat exchange and temperature reduction with the low-temperature associated gas at the outlet of the throttling expansion unit through a gas heat exchanger, and then is further subjected to temperature reduction and pressure reduction through a throttling expansion valve, so that C5+ components in the associated gas are liquefied; the liquid hydrocarbon in the associated gas is completely removed by a low-temperature associated gas inlet-liquid separator at the outlet of the throttle expansion valve through a coalescing filter, and the liquid phase is connected with a liquid phase pipeline of a compressor unit and then is sent to a liquid closed discharge tank; exchanging heat between the low-temperature outlet associated gas and the inlet associated gas of the throttling expansion unit to recover cold energy, and heating to 40-70 ℃ by using a heater;
the associated gas at the outlet of the throttling expansion unit enters a membrane separation unit;
the membrane separation unit can be primary membrane separation or secondary membrane separation;
the first-stage membrane separation unit mainly comprises a membrane component, the residual gas is directly used as product gas to be conveyed or utilized by a downstream pipe, and the permeated gas is sent to a torch or discharged outside.
The two-stage membrane separation unit mainly comprises a two-stage membrane separation component and a low-pressure compressor; associated gas is first separated with the first stage membrane, the residual gas is first used as product gas for downstream pipeline transportation and utilization, the first stage membrane permeating gas is then pumped into the low pressure compressor to raise the pressure to the first stage membrane inlet pressure, and the first stage membrane permeating gas is finally pumped into the low pressure compressor to raise the pressure to the first stage membrane inlet pressureThen enters a secondary membrane separation unit, is further concentrated by a secondary membrane, and permeates gas (rich in CO) by the secondary membrane2) And discharging, and returning the residual gas after the secondary membrane permeation to the primary membrane inlet to realize the recycling of the associated gas.
The invention provides a membrane separation method oilfield associated gas purification method based on adsorption dehydration pretreatment, which comprises the following steps:
1) the raw material associated gas is pressurized to a certain pressure by a compressor unit;
2) the compressed associated gas enters an adsorption dehydration unit to remove water vapor, wherein the associated gas is used as regenerated gas in the adsorption process;
3) dry gas at the outlet of the adsorption tower enters a throttling expansion unit, the temperature of the associated gas is reduced through a throttling expansion valve so as to liquefy C5+ components in the associated gas, C5+ components are separated from main gas of the associated gas through a gas-liquid separator, and low-temperature associated gas at the outlet of the gas-liquid separator exchanges heat with the associated gas at a throttling expansion inlet so as to recover cold; heating the low-temperature associated gas to 40-70 ℃ by an associated gas heater;
4) the associated gas at the outlet of the heater enters a membrane separation unit, the associated gas is divided into two paths, and the residual gas (CO) is permeated by the membrane separation unit2The content is less than or equal to 3 percent) is directly used as product gas to be transported or utilized by downstream pipelines, and the membrane separation permeation gas is rich in CO2And (4) removing a torch or discharging the waste water.
In the step 1) of the method, the pressure of the compressed associated gas pressurized by the compressor unit can be 7-10MPa, the temperature can be 40-60 ℃, and the temperature can be 45 ℃;
the invention has the following beneficial effects:
the invention relates to a membrane separation method oilfield associated gas purification process and unit based on adsorption dehydration pretreatment, wherein the oilfield associated gas is subjected to adsorption dehydration and throttling expansion heavy hydrocarbon removal pretreatment, so that the efficient and stable operation of a membrane separation unit is ensured. The method for removing CO in associated gas by adopting the membrane separation method has the advantages of low energy consumption, small occupied area, light weight, simple operation and maintenance and environmental friendliness2Associated gas reaches the second-class pipe gas transmission standard, so that the recycling of the associated gas is realized, and the environmental pollution and the resource waste are avoided. And the whole system can flexibly adjust the processing capacity according to the gas quantity, and meet the requirement of processing the associated gas with large gas quantity and component fluctuation.
Drawings
Fig. 1 is a membrane separation method oilfield associated gas purification process system based on adsorption dehydration pretreatment.
FIG. 2 is a schematic view of the process flow of the adsorption dehydration unit of the present invention. Wherein, 11, 12 and 13 are dehydration towers; 14 a regeneration gas heater; 15 a regeneration gas-liquid separator; 16 dust filter; 17 a gas heat exchanger; 18 regenerating the gas cooler.
FIG. 3 is a schematic of a throttled expansion unit of the present invention. Wherein, 21 the gas heat exchanger; 22 a throttle expansion valve; 23 a gas-liquid separator; 24 a coalescing filter; 25 heater
FIG. 4 is a schematic diagram of a one-stage membrane separation unit according to the present invention. Wherein, 31 to 35 membrane modules.
FIG. 5 is a schematic diagram of a two-stage membrane separation unit according to the present invention. Wherein, 41 gas mixer; 42-49 membrane modules; 51 a washer; 52 a compressor; a 53 cooler; 54 washing device
Detailed Description
The present invention will be described below with reference to specific examples, but the present invention is not limited thereto.
The experimental methods used in the following examples are all conventional methods unless otherwise specified; reagents, materials and the like used in the following examples are commercially available unless otherwise specified.
The adsorbent in the dehydration tower is silica gel or molecular sieve
Example 1
And the associated gas with the pressure of 3bar is pressurized to 9MPa by a three-stage associated gas compressor, and each stage of compressor comprises a compressor, a cooler and a gas-liquid separator. And the separated liquid phases of the three-stage gas-liquid separator are mixed and then sent to a compressor to close a discharge tank. The gas phase pressurized by the compressor is cooled to 45 ℃ in the last compressor stage.
And (3) allowing associated gas at the outlet of the compressor to enter an adsorption dehydration unit, allowing 80% of main gas to directly enter a dehydration tower A for adsorption dehydration, allowing the rest 20% of the associated gas to pass through the dehydration tower for adsorption dehydration, heating to 180 ℃ to serve as regenerated gas for desorption dehydration in the dehydration tower A, returning to an inlet after the regeneration is completed, converging the main gas, and allowing the main gas to enter the dehydration tower for purification. And (4) introducing associated gas at the outlet of the dehydration tower into a dust filter (preventing adsorbent dust from entering the next stage) for dust removal. The content of associated gas water is reduced to 50ppm after dehydration in a dehydration tower.
And the associated gas at the outlet of the adsorption dehydration unit enters a throttling expansion unit. The associated gas at the inlet of the throttling expansion unit is subjected to heat exchange and temperature reduction through a heat exchanger, and then is subjected to temperature reduction and pressure reduction through a throttling expansion valve to 6MPa and 13 ℃, so that the C5+ component in the associated gas is partially liquefied; the low-temperature associated gas at the outlet of the throttle expansion valve enters a gas-liquid separator to completely remove liquid hydrocarbon in the associated gas, and a liquid phase is connected with a compressor unit for liquid phase management and enters a liquid closed discharge tank; the low-temperature outlet associated gas exchanges heat with the associated gas at the inlet of the throttling expansion unit to recover cold energy, and the temperature of the associated gas is raised to 55 ℃ by a heater.
The associated gas at the outlet of the throttling expansion unit enters a primary membrane separation unit, the associated gas is separated by a primary membrane, and the residual gas (CO) is permeated2The content is less than or equal to 3 percent) reaches the second-class pipeline transportation standard of natural gas and is directly used as product gas to be transported to downstream pipelines; the first-stage membrane permeation gas is sent to a torch.
Example 2
The associated gas with the pressure of 3.2MPa is pressurized to 8.8MPa by a first-stage natural gas compressor, and each stage of compressor comprises a compressor, a cooler and a gas-liquid separator. And the separated liquid phases of the three-stage gas-liquid separator are mixed and then sent to a compressor to close a discharge tank. The gas phase pressurized by the compressor is cooled to 40 ℃ in the last compressor stage.
And (3) allowing associated gas at the outlet of the compressor to enter an adsorption dehydration unit, allowing 80% of main gas to directly enter a dehydration tower A for adsorption dehydration, allowing the rest 20% of the associated gas to pass through the dehydration tower for adsorption dehydration, heating to 180 ℃ to serve as regenerated gas for desorption dehydration in the dehydration tower A, returning to an inlet after the regeneration is completed, converging the main gas, and allowing the main gas to enter the dehydration tower for purification. And (4) introducing associated gas at the outlet of the dehydration tower into a dust filter (preventing adsorbent dust from entering the next stage) for dust removal. The content of associated gas water is reduced to 50ppm after dehydration by an adsorption tower.
And the associated gas at the outlet of the adsorption dehydration unit enters a throttling expansion unit. The associated gas at the inlet of the throttling expansion unit is subjected to heat exchange and temperature reduction through a heat exchanger, and then is subjected to temperature reduction and pressure reduction through a throttling expansion valve to 4.5MPa and 8 ℃ so that the C5+ component in the associated gas is partially liquefied; the low-temperature associated gas at the outlet of the throttle expansion valve enters a gas-liquid separator to completely remove liquid hydrocarbon in the associated gas, and a liquid phase is connected with a compressor unit for liquid phase management and enters a liquid closed discharge tank; the low-temperature outlet associated gas exchanges heat with the associated gas at the inlet of the throttling expansion unit to recover cold energy, and the temperature of the associated gas is raised to 55 ℃ by a heater.
And an associated gas secondary membrane separation unit at the outlet of the throttling expansion unit. Separating associated gas with first-stage membrane, and permeating residual gas (CO)2The content is less than or equal to 3 percent) reaches the second-class pipeline transportation standard of natural gas and is directly used as product gas to be transported to downstream pipelines; the first-stage membrane permeation gas continuously enters a low-pressure compressor to increase the pressure to 4.5 MPa; then enters a secondary membrane separation unit, is further concentrated by a secondary membrane, and permeates gas (rich in CO) by the secondary membrane2) And discharging, and returning the residual gas after the secondary membrane permeation to the primary membrane inlet to realize the recycling of the associated gas.
The above embodiments are merely illustrative of the technical ideas and features of the present invention, and the purpose of the embodiments is to enable those skilled in the art to understand the contents of the present invention and implement the present invention, and not to limit the protection scope of the present invention. All equivalent changes and modifications made according to the spirit of the present invention should be covered within the protection scope of the present invention.
The invention is not the best known technology.
Claims (5)
1. A membrane separation method oilfield associated gas purification system based on adsorption dehydration pretreatment comprises a compressor unit, an adsorption dehydration unit, a throttling expansion unit and a membrane separation unit which are sequentially connected with a feed gas;
the compressor unit is used for pressurizing associated gas to a certain pressure,
the compressor unit is a first-stage, second-stage or third-stage compressor unit,
wherein each stage of compressor unit comprises a compressor, a cooler and a gas-liquid separator;
the pressure of the compressed associated gas compressed by the last stage of compressor unit is 7-10MPa, and the temperature is 40-60 ℃;
the compressed associated gas compressed by the last stage of compressor unit enters an adsorption dehydration unit;
all liquid phase outlets of the gas-liquid separators of the compressor unit are connected with the discharge tank after being mixed;
the adsorption dehydration unit adopts an isobaric temperature swing adsorption process and consists of a dehydration tower, a regeneration gas heater, a regeneration gas cooler, a regeneration gas-liquid separator and a dust filter;
the method comprises the following steps that associated gas at the outlet of a compressor is divided into two streams by an adjusting valve, one stream of the associated gas is 10-25% used as regenerated gas, the associated gas returns to an inlet after the regeneration work is finished and is converged with the other stream of process gas of 75-90%, and the combined gas enters a dehydration tower to be purified;
namely, compressed associated gas accounting for 75-90% of the total amount is directly sent to a dehydration tower through a program control valve, under the selective adsorption of an adsorbent bed layer in the dehydration tower, moisture in the gas is adsorbed, the gas which is not adsorbed is purified, and the gas enters a dust filter for dust removal through the program control valve;
after the residual associated gas is adsorbed and dehydrated by a dehydrating tower, the residual associated gas is heated by a regenerated gas heater to be used as an adsorbent in a regenerated gas desorption dehydrating tower, the regenerated gas rich in water vapor is cooled to 40-50 ℃ by a regenerated gas cooler, liquid water and gas in the gas discharged from the regenerated gas cooler are separated by a regenerated gas-gas liquid separator, and the separated gas returns to an inlet to be converged with the main gas and enters the dehydrating tower to be purified;
the gas content of associated gas at the outlet of the adsorption dehydration unit is reduced to 50 ppm;
and the associated gas at the outlet of the adsorption dehydration unit enters a throttling expansion unit.
2. The system of claim 1, wherein: the throttling expansion unit comprises a gas heat exchanger, a throttling expansion valve, a gas-liquid separator, a coalescing filter and a heater;
the associated gas at the inlet of the throttling expansion unit exchanges heat with the low-temperature associated gas at the outlet of the throttling expansion unit through a gas heat exchanger to reduce the temperature, and then is further reduced in temperature and pressure through the throttling expansion valve to liquefy C5+ components in the associated gas; the liquid hydrocarbon in the associated gas is completely removed by a low-temperature associated gas inlet-liquid separator at the outlet of the throttle expansion valve through a coalescing filter, and the liquid phase is connected with a liquid phase pipeline of a compressor unit and then is sent to a liquid closed discharge tank; the low-temperature outlet associated gas exchanges heat with the associated gas at the inlet of the throttling expansion unit to recover cold energy, and the temperature is raised to 40-70 ℃ through a heater;
and the associated gas at the outlet of the throttling expansion unit enters a membrane separation unit.
3. The system of claim 1, wherein: the membrane separation unit is primary membrane separation or secondary membrane separation;
the first-stage membrane separation unit mainly comprises a membrane component, the residual gas is directly used as product gas to be conveyed or utilized by a downstream pipe, and the permeation gas is sent to a torch or discharged;
the two-stage membrane separation unit mainly comprises a two-stage membrane separation component and a low-pressure compressor; associated gas is firstly separated by a first-stage membrane, the residual gas is directly conveyed or utilized as product gas to a downstream pipe, the first-stage membrane permeation gas continuously enters a low-pressure compressor to increase the pressure to the pressure of a first-stage membrane inlet, then enters a second-stage membrane separation unit, is further concentrated by a second-stage membrane, the second-stage membrane permeation gas is discharged outside, and the secondary membrane permeation residual gas returns to the first-stage membrane inlet to realize the recycling of the associated gas.
4. A membrane separation method oilfield associated gas purification method based on adsorption dehydration pretreatment comprises the following steps:
1) pressurizing raw material associated gas by a compressor unit;
2) the compressed associated gas enters an adsorption dehydration unit to remove water vapor, wherein the associated gas is used as regenerated gas in the adsorption process;
3) dry gas at the outlet of the adsorption tower enters a throttling expansion unit, the temperature of the associated gas is reduced through a throttling expansion valve so as to liquefy C5+ components in the associated gas, C5+ components are separated from main gas of the associated gas through a gas-liquid separator, and low-temperature associated gas at the outlet of the gas-liquid separator exchanges heat with the associated gas at a throttling expansion inlet so as to recover cold; heating the low-temperature associated gas to 40-70 ℃ by an associated gas heater;
4) associated gas at the outlet of the heater enters a membrane separation unit, the associated gas is divided into two paths, the residual gas of the membrane separation unit is directly used as product gas to be conveyed or utilized by a downstream pipe, and the permeation gas of the membrane separation unit is rich in CO2And (4) removing a torch or discharging the waste water.
5. The method of claim 4, wherein: in the step 1), the pressure of the compressed associated gas pressurized by the compressor unit is 7-10MPa, and the temperature is 40-60 ℃.
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