CN212504757U - Flash gas decarbonization and dehydration device - Google Patents
Flash gas decarbonization and dehydration device Download PDFInfo
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- CN212504757U CN212504757U CN202021057244.0U CN202021057244U CN212504757U CN 212504757 U CN212504757 U CN 212504757U CN 202021057244 U CN202021057244 U CN 202021057244U CN 212504757 U CN212504757 U CN 212504757U
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Abstract
The utility model relates to a natural gas processing and processing technology field is a flash distillation gas decarbonization dewatering device, and it includes flash tank, defoaming jar, heat energy recoverer, air cooler, vapour and liquid separator, fine filter, heat exchanger, membrane separation subassembly, and the fixed intercommunication in flash tank middle part import has the feed liquor pipeline, and fixed intercommunication has filter discharging pipeline between fine filter export and the import of heat energy recoverer top. The utility model has the advantages of reasonable and compact structure, convenient to use, it can carry out one-step method decarbonization dehydration to the rich liquid flash distillation gas that natural gas decarbonization process produced, can make the rich liquid recycling after handling, and the flash distillation dry gas after the processing can use as fuel gas high-efficiently, safely, has solved the problem that flash distillation gas treatment running cost is high, the management maintenance degree of difficulty is big and the low heat value is difficult to the utilization, has safety, laborsaving, simple and convenient, efficient characteristics.
Description
Technical Field
The utility model relates to a natural gas treatment and processing technology field is a flash distillation gas decarbonization dewatering device.
Background
Natural gas is widely used as a clean energy source, and in order to meet the rapidly growing demand for natural gas, in recent years, high carbon content gas fields are increasingly developed, such as domestic Jilin ChangLing gas fields, Daqing Xushen gas fields, Zhonghai oil east gas fields, Zhongpetrochemical Sonnan gas fields, Tarim Akema wood gas fields and the like, and according to the requirement of commodity gas quality export standards, raw gas treatment needs to be decarbonized (desulfurized)The main process for treating natural gas decarburization in gas fields at home and abroad still takes an alcohol amine method as a main process at present, and absorbs CO for meeting the requirement of recycling2The alcohol amine solution (rich solution) needs to be regenerated after pressure reduction and flash evaporation, while part of flash evaporation gas can be generated in the pressure reduction process of the rich solution, and the flash evaporation gas has low pressure (0.8 MPa to 1.4 MPa), high temperature and high CO content2（CO240-70% volume content), and if the barren solution is used for reabsorption, the circulation amount is large, the energy consumption is high, and the effect is poor.
The first method is that the raw material gas is pressurized by a compressor and then returns to a raw material gas inlet to enter a decarburization absorption tower; the second is to discharge the burning through a low-pressure discharge torch system; and the third is blending into fuel gas system. Although the first mode can better solve the problem of the outlet of flash evaporation gas, a compressor needs to be additionally arranged, so that the investment is high, the energy consumption is high, the equipment is more, the management and maintenance difficulty is high, and the operation cost is high (reaching 0.5 yuan/cubic); in the second mode, because the flash evaporation gas has high temperature (65-85 ℃), high carbon content and saturated water content, a large amount of free water can be separated out due to temperature drop in the emptying process, and finally accumulated in a pipeline, so that the pipeline corrosion can be accelerated, the freezing and blocking can be easily caused in winter, the potential safety hazard is large, and the high CO content is high2The phenomenon of incomplete combustion can exist, and the phenomena of environmental pollution and resource waste can be caused; the third mode is not blended into a fuel gas system by decarburization dehydration treatment, because CO2The content is high, the calorific value of the fuel gas is reduced after mixing, the efficiency of the fuel gas equipment is influenced, the heat load is insufficient, the stable operation of a heating system of a treatment plant is influenced, the flash steam is saturated and contains water, the freezing blockage is very easy to cause, and the whole fuel gas system (including the fuel gas equipment) needs to be selected and used for resisting CO for avoiding corrosion2The material(s) of (2) will result in increased investment.
Disclosure of Invention
The utility model provides a flash distillation gas decarbonization dewatering device has overcome above-mentioned prior art not enough, and it can effectively solve rich liquid flash distillation gas decarbonization dehydration investment height, energy consumption height, equipment are many, freeze stifled, pollute, the management maintenance degree of difficulty is big and there is the problem of great potential safety hazard in the current natural gas decarbonization device.
The technical scheme of the utility model is realized through following measure: a flash gas decarbonization and dehydration device comprises a flash tank, a defoaming tank, a heat energy recoverer, an air cooler, a gas-liquid separator, a fine filter, a heat exchanger and a membrane separation assembly, wherein a liquid inlet pipeline is fixedly communicated with an inlet in the middle of the flash tank, a regeneration pipeline is fixedly communicated with an outlet in the bottom of the flash tank, the defoaming tank is seated on the flash tank, an outlet in the top of the flash tank is fixedly communicated with an inlet in the bottom of the defoaming tank, a heat energy recovery feeding pipeline is fixedly communicated between an outlet in the top of the defoaming tank and an inlet in the middle of the heat energy recoverer, a heat energy recovery discharging pipeline is fixedly communicated between an outlet in the middle of the heat energy recoverer and an inlet in the middle of the air cooler, an air cooler discharging pipeline is fixedly communicated between an outlet in the middle of the air cooler and an inlet in the middle of, a filter discharge pipeline is fixedly communicated between an outlet of the fine filter and an inlet at the top of the heat energy recoverer, a circulating feed pipeline is fixedly communicated with an inlet at the bottom of the heat exchanger, a circulating discharge pipeline is fixedly communicated with an outlet at the bottom of the heat exchanger, a heat exchanger feed pipeline is fixedly communicated between an outlet at the bottom of the heat energy recoverer and an inlet at the middle of the heat exchanger, a membrane separation feed pipeline is fixedly communicated between an outlet at the middle of the heat exchanger and an inlet at the middle of the membrane separation assembly, a membrane separation discharge pipeline is fixedly communicated with an outlet at the middle of the membrane separation assembly, a liquid discharge pipeline is fixedly communicated with the membrane separation feed pipeline, an acid gas removal system pipeline is fixedly communicated with the membrane separation feed pipeline, an air discharge pipeline is fixedly communicated with the acid gas removal system pipeline, and an air discharge pipeline, and a compressed air pipeline is fixedly communicated with the membrane separation feed pipeline between the inlet of the liquid discharge.
The following are further optimization or/and improvement of the technical scheme of the utility model:
the heat energy recoverer and the heat exchanger are both of a pipe shell structure.
The membrane separation module is a hollow fiber membrane.
And a check valve is fixedly arranged on the compressed air pipeline.
CO is fixedly arranged on the heat energy recovery feeding pipeline2The analyzer is characterized in that a CO separation discharge pipe line between the middle outlet of the membrane separation component and the inlet of the first emptying pipeline is fixedly provided with a CO2An analyzer.
The utility model has the advantages of reasonable and compact structure, convenient to use, it can carry out one-step method decarbonization dehydration to the rich liquid flash distillation gas that natural gas decarbonization process produced, can make the rich liquid recycling after handling, and the flash distillation dry gas after the processing can use as fuel gas high-efficiently, safely, has solved the problem that flash distillation gas treatment running cost is high, the management maintenance degree of difficulty is big and the low heat value is difficult to the utilization, has safety, laborsaving, simple and convenient, efficient characteristics.
Drawings
FIG. 1 is a schematic process flow diagram of the preferred embodiment of the present invention.
The codes in the figures are respectively: 1 is a flash tank, 2 is a defoaming tank, 3 is a heat energy recoverer, 4 is an air cooler, 5 is a gas-liquid separator, 6 is a fine filter, 7 is a heat exchanger, 8 is a membrane separation assembly, 9 is a liquid inlet pipeline, 10 is a regeneration pipeline, 11 is a heat energy recovery feed pipeline, 12 is a heat energy recovery discharge pipeline, 13 is an air cooler discharge pipeline, 14 is a separator discharge pipeline, 15 is a filter feed pipeline, 16 is a filter discharge pipeline, 17 is a circulation feed pipeline, 18 is a circulation discharge pipeline, 19 is a heat exchanger feed pipeline, 20 is a membrane separation feed pipeline, 21 is a membrane separation discharge pipeline, 22 is a liquid discharge pipeline, 23 is a deacidification gas system pipeline, 24 is a first emptying pipeline, 25 is a second emptying pipeline, 26 is an air pipe compression pipeline, 27 is a one-way valve, 28 is CO2An analyzer.
Detailed Description
The utility model discloses do not receive the restriction of following embodiment, can be according to the utility model discloses a technical scheme and actual conditions determine concrete implementation.
In the present invention, for convenience of description, the description of the relative position relationship of the components is described according to the layout mode of the attached drawing 1 in the specification, such as: the positional relationship of front, rear, upper, lower, left, right, etc. is determined in accordance with the layout direction of fig. 1 of the specification.
The invention will be further described with reference to the following examples and drawings:
as shown in the attached figure 1, the flash gas decarburization dehydration device comprises a flash tank 1, a defoaming tank 2, a heat energy recoverer 3, an air cooler 4, a gas-liquid separator 5, a fine filter 6, a heat exchanger 7 and a membrane separation assembly 8, wherein a liquid inlet pipeline 9 is fixedly communicated with an inlet in the middle of the flash tank 1, a regeneration pipeline 10 is fixedly communicated with an outlet in the bottom of the flash tank 1, the defoaming tank 2 is seated on the flash tank 1, an outlet in the top of the flash tank 1 is fixedly communicated with an inlet in the bottom of the defoaming tank 2, a heat energy recovery feeding pipeline 11 is fixedly communicated between the outlet in the top of the defoaming tank 2 and an inlet in the middle of the heat energy recoverer 3, a heat energy recovery discharging pipeline 12 is fixedly communicated between the outlet in the middle of the heat energy recoverer 3 and the inlet in the middle of the air cooler 4, an air cooler discharging pipeline 13 is fixedly communicated between the, a filter feeding pipeline 15 is fixedly communicated between an outlet at the top of the gas-liquid separator 5 and an inlet of the fine filter 6, a filter discharging pipeline 16 is fixedly communicated between an outlet of the fine filter 6 and an inlet at the top of the heat energy recoverer 3, a circulating feeding pipeline 17 is fixedly communicated between an inlet at the bottom of the heat exchanger 7, a circulating discharging pipeline 18 is fixedly communicated between an outlet at the bottom of the heat exchanger 7 and an inlet at the middle of the heat exchanger 7, a heat exchanger feeding pipeline 19 is fixedly communicated between an outlet at the middle of the heat exchanger 7 and an inlet at the middle of the membrane separation assembly 8, a membrane separation feeding pipeline 20 is fixedly communicated between an outlet at the middle of the membrane separation assembly 8, a membrane separation discharging pipeline 21 is fixedly communicated with an outlet at the middle of the membrane separation assembly 8, a liquid discharging pipeline 22 is fixedly communicated with the membrane separation feeding pipeline 20, an acid gas removing system pipeline 23 is fixedly, a second vent pipeline 25 is fixedly communicated between the acid gas removal system pipeline 23 and the first vent pipeline 24, and a compressed air pipeline 26 is fixedly communicated on the membrane separation feeding pipeline 20 between the inlet of the liquid discharge pipeline 22 and the inlet of the middle part of the membrane separation assembly 8.
The utility model discloses in, the mountable is reserveWhen one membrane separation module 8 is regenerated, the other membrane separation module 8 can be continuously used, so that the normal operation of the membrane separation process is ensured. The flash tank 1 and the defoaming tank 2 can be integrated together, the length of the defoaming tank 2 can be 0.5m to 1.0m, the nominal diameter of the defoaming tank 2 is usually 5 times to 8 times of the diameter of a pipeline, the nominal diameter is not less than 200mm, and CO resistance is arranged in the defoaming tank 22The outlet of the defoaming tank 2 can be provided with a sampling port or CO2An analyzer 28. The fine filter 6 and the gas-liquid separator 5 can be integrated, the fine filter 6 can be a filter element made of glass fiber and microfiber, and the fine filter 6 can filter liquid drops with the precision of 0.1-0.5 μm. The utility model discloses flash distillation gas decarbonization dewatering device can install thermometer, flowmeter, manometer, control valve, sled dress base as required and come safe effectual rich solution flash distillation gas to carry out the decarbonization dehydration more.
In the prior art, rich liquid flash gas in a natural gas decarbonization device has high decarbonization and dehydration investment, high energy consumption, more equipment, high treatment and operation cost, high management and maintenance difficulty and great potential safety hazard; the utility model discloses, according to rich liquid flash distillation gas temperature height, low pressure, saturated moisture, high carbonous and smuggle characteristics such as foam secretly, in addition the factory fuel gas need be followed outer defeated product gas and got gas, outer defeated atmospheric pressure is higher usually, need the pressure regulating rear can regard as the fuel gas, pressure can not obtain better utilization, based on looks attitude balance and membrane separation combination processing apparatus, adopt the defoaming, the air cooling, preseparation, filtration, heat transfer and membrane separation combination process technology, realize the one-step method decarbonization to rich liquid flash distillation gas, the dehydration, flash distillation dry gas after the processing can be high-efficient, use as the fuel gas safely, rich liquid after the processing can recycle, energy-concerving and environment-protective. The utility model discloses flash distillation gas decarbonization dewatering device passes through heat transfer network optimization and energy step utilization, accomplishes the energy high efficiency and utilizes, the at utmost realized energy saving and consumption reduction, the utility model discloses arrange according to process flow and optimum water conservancy and thermodynamics and carry out organic combination for mechatronic high integration possesses automatic control, remote monitoring.
The flash evaporation gas decarbonization and dehydration device can be further optimized or/and improved according to actual needs:
as shown in fig. 1, the heat energy recoverer 3 and the heat exchanger 7 are both of a tube-and-tube structure. The heat exchanger 7 can use heat conducting oil or steam as a heat source. The temperature of the flash evaporation gas of the rich solution is between 65 and 85 ℃, when the temperature of the flash evaporation gas is higher and reaches between 75 and 85 ℃, the temperature of the gas output from the heat energy recoverer 3 can reach between 70 and 80 ℃, according to the actual situation, the heat exchanger 7 can be eliminated, and the gas output from the heat energy recoverer 3 can directly enter the membrane separation component 8 for treatment.
As shown in fig. 1, the membrane separation module 8 is a hollow fiber membrane. The membrane separation module 8 can be selected from a hollow fiber membrane special for decarburization and having a diameter of 130mm and a length of 1100mm, and when the amount of the treated gas is 25000m3When the pressure is 1.0MPa to 1.2MPa, 10 membranes can be selected to run in parallel, the yield of product gas methane in the membrane separation feed pipeline 20 can reach 90 percent to 95 percent, the water dew point can be minus 5 ℃ to minus 10 ℃, and the gas outlet of the membrane separation component 8 can be provided with a sampling port, a water dew point analyzer or a CO dew point analyzer2The analyzer 28 can increase or decrease the number of membranes in the membrane separation module 8 according to the methane yield and the water dew point requirement, so as to grasp the gas outlet CO of the membrane separation module 82Content, better control the decarburization effect. When membrane separation module 8 is being regenerated, the gas in membrane separation feed line 20 may be discharged by drain line 22 to a low pressure flare system for flare.
As shown in fig. 1, a check valve 27 is fixedly mounted on the compressed air line 26. The check valve 27 allows one-way flow of compressed air in the compressed air line 26 to prevent gas in the membrane separation feed line 20 from flowing into the compressed air line 26. Compressed air or nitrogen can be introduced into the compressed air pipeline 26 to regenerate the membrane separation component 8, the pressure of the compressed air or nitrogen can be 0.4MPa to 1.0MPa, the temperature for regenerating the membrane separation component 8 can be 60 ℃ to 80 ℃, and the treatment gas quantity of a single group of membranes is 2000m3Calculated as/d, the regeneration gas content of the membrane separation module 8 can be 20m at a temperature of 20 ℃ and a pressure of 101.325kPa3H to 50m3The regeneration period can be 3d to 5 d.
As shown in the attached FIG. 1, CO is fixedly installed on a heat energy recovery feeding pipeline 112Analyzer 28, MembraneA CO separation discharging pipeline 21 between the middle outlet of the separation component 8 and the inlet of the first emptying pipeline 24 is fixedly provided with a CO separation discharging pipeline2An analyzer 28. CO 22The analyzer 28 may monitor CO2The content of the component (A) ensures that the decarburization process is normally carried out.
The utility model discloses a flash distillation gas is handled and membrane regeneration two parts, can confirm whether need set up regeneration flow or adopt removable according to operating condition, and the roping can adopt the sled dress structure to mill's regeneration, and convenient operation maintains simply, and membrane separation subassembly 8 can be regenerated and used, abundant resources are saved, and is safe high-efficient, economical and practical. The utility model discloses a device mainly used high carbon-containing gas field decarbonization process rich liquid flash distillation gas's decarbonization dehydration also can be used in the single well or gathering occasions such as station yard that need decarbonization, dehydration similar with this operating mode, has very wide application prospect.
Above technical feature constitutes the utility model discloses a best embodiment, it has stronger adaptability and best implementation effect, can increase and decrease unnecessary technical feature according to actual need, satisfies the demand of different situation.
The utility model discloses best embodiment's use: rich liquid generated by a natural gas decarbonization device enters a flash tank 1 for pressure reduction and flash evaporation, liquid obtained after flash evaporation is discharged from a regeneration pipeline 10 and can be discharged to a rich liquid regeneration system for recycling, flash vapor with the pressure of 0.8MPa to 1.4MPa and the temperature of 65 ℃ to 85 ℃ obtained after flash evaporation enters a defoaming tank 2 for defoaming, the flash vapor after defoaming enters a tube pass of a heat energy recoverer 3 for heat exchange and is cooled to 50 ℃ to 60 ℃, then enters an air cooler 4 from a heat energy recovery discharge pipeline 12 for further cooling to 20 ℃ to 35 ℃, the flash vapor cooled in the air cooler 4 enters a gas-liquid separator 5 for gas-liquid separation, liquid separated in the gas-liquid separator 5 is discharged from a separator discharge pipeline 14 and can be discharged to a rich liquid regeneration system for recycling, gas separated in the gas-liquid separator 5 enters a fine filter 6 from a filter feed pipeline 15, and gas filtered by the fine filter 6 enters a shell pass of the heat energy recoverer 3 and enters a heat energy recovery feed pipeline 11 The flash steam after foam removal in the tube pass of the heat energy recoverer 3 is subjected to heat exchange, and the steam after heat exchange and temperature rise in the heat energy recoverer 3The gas enters a heat exchanger 7 to be continuously heated to 60-65 ℃, the heated gas enters a membrane separation assembly 8 from a membrane separation feed pipeline 20 for separation, and the water-containing CO separated from the membrane separation assembly 82The tail gas is discharged from a deacidification gas system pipeline 23, and the fuel gas separated from the membrane separation assembly 8 is discharged from a membrane separation discharge pipeline 21 and can enter a fuel gas system for use.
Claims (5)
1. A flash evaporation gas decarburization dehydration device is characterized by comprising a flash evaporation tank, a defoaming tank, a heat energy recoverer, an air cooler, a gas-liquid separator, a fine filter, a heat exchanger and a membrane separation assembly, wherein a liquid inlet pipeline is fixedly communicated with an inlet in the middle of the flash evaporation tank, a regeneration pipeline is fixedly communicated with an outlet in the bottom of the flash evaporation tank, the defoaming tank is arranged on the flash evaporation tank, an outlet in the top of the flash evaporation tank is fixedly communicated with an inlet in the bottom of the defoaming tank, a heat energy recovery feeding pipeline is fixedly communicated between an outlet in the top of the defoaming tank and an inlet in the middle of the heat energy recoverer, a heat energy recovery discharging pipeline is fixedly communicated between an outlet in the middle of the heat energy recoverer and an inlet in the middle of the air cooler, an air cooler discharging pipeline is fixedly communicated between an outlet in the middle of the air cooler and an inlet, a filter discharge pipeline is fixedly communicated between an outlet of the fine filter and an inlet at the top of the heat energy recoverer, a circulating feed pipeline is fixedly communicated with an inlet at the bottom of the heat exchanger, a circulating discharge pipeline is fixedly communicated with an outlet at the bottom of the heat exchanger, a heat exchanger feed pipeline is fixedly communicated between an outlet at the bottom of the heat energy recoverer and an inlet at the middle of the heat exchanger, a membrane separation feed pipeline is fixedly communicated between an outlet at the middle of the heat exchanger and an inlet at the middle of the membrane separation assembly, a membrane separation discharge pipeline is fixedly communicated with an outlet at the middle of the membrane separation assembly, a liquid discharge pipeline is fixedly communicated with the membrane separation feed pipeline, an acid gas removal system pipeline is fixedly communicated with the membrane separation feed pipeline, an air discharge pipeline is fixedly communicated with the acid gas removal system pipeline, and an air discharge pipeline, and a compressed air pipeline is fixedly communicated with the membrane separation feed pipeline between the inlet of the liquid discharge.
2. The flash gas decarburization dehydration device according to claim 1, wherein the heat energy recoverer and the heat exchanger are both of a tube-and-tube structure.
3. The flash gas decarbonization and dehydration device of claim 2, wherein the membrane separation module is a hollow fiber membrane.
4. The flash gas decarbonization and dehydration apparatus of claim 3 wherein a check valve is fixedly mounted on the compressed air line.
5. The flash gas decarbonization and dehydration device according to claim 1 or 2, characterized in that the CO recycling feed line is fixedly provided with a CO2The analyzer is characterized in that a CO separation discharge pipe line between the middle outlet of the membrane separation component and the inlet of the first emptying pipeline is fixedly provided with a CO2An analyzer.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021057244.0U CN212504757U (en) | 2020-06-10 | 2020-06-10 | Flash gas decarbonization and dehydration device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021057244.0U CN212504757U (en) | 2020-06-10 | 2020-06-10 | Flash gas decarbonization and dehydration device |
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| CN212504757U true CN212504757U (en) | 2021-02-09 |
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| CN202021057244.0U Active CN212504757U (en) | 2020-06-10 | 2020-06-10 | Flash gas decarbonization and dehydration device |
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| CN (1) | CN212504757U (en) |
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Effective date of registration: 20210319 Address after: 100120 No.6 liupukang street, Xicheng District, Beijing Patentee after: CHINA NATIONAL PETROLEUM Corp. Patentee after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Patentee after: CNPC (XINJIANG) PETROLEUM ENGINEERING Co.,Ltd. Address before: 100032 No.6 liupukang street, Xicheng District, Beijing Patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Patentee before: CNPC (XINJIANG) PETROLEUM ENGINEERING Co.,Ltd. |