CN108977247B - Integrated TEG dehydration integrated process device and method - Google Patents
Integrated TEG dehydration integrated process device and method Download PDFInfo
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- CN108977247B CN108977247B CN201811068723.XA CN201811068723A CN108977247B CN 108977247 B CN108977247 B CN 108977247B CN 201811068723 A CN201811068723 A CN 201811068723A CN 108977247 B CN108977247 B CN 108977247B
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- 238000000034 method Methods 0.000 title claims abstract description 39
- 230000018044 dehydration Effects 0.000 title claims abstract description 31
- 238000006297 dehydration reaction Methods 0.000 title claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 107
- 238000010521 absorption reaction Methods 0.000 claims abstract description 36
- 238000001914 filtration Methods 0.000 claims abstract description 12
- 239000007791 liquid phase Substances 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 101
- 230000001502 supplementing effect Effects 0.000 claims description 28
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 26
- 239000002737 fuel gas Substances 0.000 claims description 25
- 238000011084 recovery Methods 0.000 claims description 23
- 239000002699 waste material Substances 0.000 claims description 23
- 238000001704 evaporation Methods 0.000 claims description 20
- 230000008020 evaporation Effects 0.000 claims description 20
- 239000000047 product Substances 0.000 claims description 20
- 230000008929 regeneration Effects 0.000 claims description 20
- 238000011069 regeneration method Methods 0.000 claims description 20
- 230000001105 regulatory effect Effects 0.000 claims description 19
- 239000002912 waste gas Substances 0.000 claims description 16
- 239000003345 natural gas Substances 0.000 claims description 13
- 238000004064 recycling Methods 0.000 claims description 11
- 238000002485 combustion reaction Methods 0.000 claims description 9
- 239000012535 impurity Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 4
- 239000007857 degradation product Substances 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 239000000567 combustion gas Substances 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 2
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 129
- 230000010354 integration Effects 0.000 description 7
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 3
- 230000002457 bidirectional effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 150000002334 glycols Chemical class 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/1431—Pretreatment by other processes
- B01D53/145—Pretreatment by separation of solid or liquid material
-
- 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
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses an integrated TEG dehydration integrated process device and a method, wherein the device comprises a raw gas filtering separator, a TEG absorption tower and a dry gas/lean liquid heat exchanger which are connected in sequence; the liquid phase outlet of the bottom of the TEG absorption tower is connected with a TEG circulating pump; the rich liquid outlet of the TEG circulating pump is sequentially connected with a rich liquid heat exchange coil, a flash tank, a TEG solution filter, a lean/rich liquid heat exchanger, a lean liquid buffer tank and a rich liquid rectifying column; the flash gas outlet of the flash tank is connected with a TEG fire tube type reboiler; the rich liquid rectifying column is connected with the fire tube type reboiler, the lean liquid rectifying column and the lean liquid buffer tank; the lean solution buffer tank outlet, the lean/rich solution heat exchanger, the TEG circulating pump, the dry gas/lean solution heat exchanger shell side and the TEG absorption tower top liquid phase inlet are sequentially connected. The invention not only makes the process simpler, is more beneficial to highly integrated design and easy to move, but also saves energy and reduces emission to a great extent, reduces the operation cost and reduces the disposable investment.
Description
Technical Field
The invention relates to a novel, efficient and energy-saving integrated TEG dehydration process, and belongs to the technical field of dehydration processes in the fields of natural gas treatment plants, natural gas single-well trial production, shale gas dehydration stations and the like.
Background
TEG dehydration is based on the absorption principle, in which a hydrophilic liquid is countercurrently contacted with natural gas, so as to remove water vapor in the gas. For dehydration by the glycol method, the triethylene glycol has the best economic benefit among various glycol compounds due to large dew point drop, low cost and reliable operation. And thus is widely used abroad. When the dehydration of triethylene glycol and the dehydration of a solid adsorbent can meet the dew point drop requirement, the dehydration of triethylene glycol has better economic benefit. Compared with adsorption dehydration, glycol dehydration has the advantages of low investment, small pressure drop, stable operation, simple maintenance of the device and the like, and therefore, the glycol dehydration has been widely applied in occasions with low water dew point requirements. However, in practical applications, the conventional TEG absorption process still needs to be improved in the following areas:
① The stripping method is adopted for regeneration, and the regenerated stripping gas is burnt and discharged, so that on one hand, energy waste is caused, and on the other hand, the environment is polluted to a certain extent;
② The process flow is complex, the equipment is more, and the integration degree of the device is not high;
③ In the traditional waste liquid recovery process by gravity, the recovery tank is arranged below the ground, so that skid-mounted and relocation are not easy to carry out;
Disclosure of Invention
In order to overcome the defects of the prior art, improve the integration of a TEG dehydration device and reduce the regeneration energy consumption, the invention provides an efficient and energy-saving TEG dehydration process, which realizes the direct internal utilization of a rich liquid flash gas and a TEG regeneration waste gas, and simultaneously optimizes and improves the recovery and recycling flow of TEG waste liquid. The treatment process of the invention is more energy-saving and environment-friendly, and reduces the operation cost and the one-time investment.
The technical scheme adopted by the invention is as follows: an integrated TEG dehydration integrated process device comprises a raw material gas filtering separator, a TEG absorption tower and a dry gas/lean liquid heat exchanger which are connected in sequence; a liquid phase outlet at the bottom of the TEG absorption tower is connected with a TEG circulating pump; the rich liquid outlet of the TEG circulating pump is sequentially connected with a rich liquid heat exchange coil, a flash tank, a TEG solution filter, a lean/rich liquid heat exchanger, a lean liquid buffer tank and a rich liquid rectifying column; the flash gas outlet of the flash tank is connected with a TEG fire tube type reboiler; the rich liquid rectifying column is connected with the fire tube type reboiler, the lean liquid rectifying column and the lean liquid buffer tank; the lean solution buffer tank outlet, the lean/rich solution heat exchanger, the TEG circulating pump, the dry gas/lean solution heat exchanger shell side and the TEG absorption tower top liquid phase inlet are sequentially connected.
The invention also provides an integrated TEG dehydration integrated process method, which comprises the following steps:
1. Absorption heat exchange and output of wet purified gas:
The method comprises the steps that raw natural gas enters a filtering separator to remove mechanical impurities carried in the raw gas, then enters the lower part of a TEG absorption tower, and is in countercurrent contact with TEG lean solution from bottom to top in the tower, saturated water in the natural gas is removed, and product gas after moisture removal enters a dry gas/lean solution heat exchanger to exchange heat with the lean TEG solution and then is output as product gas;
2. TEG solution circulation comprises flash evaporation, filtration, heat exchange and regeneration of rich solution, heat exchange and circulation reinjection of lean solution:
the TEG rich liquid from the lower part of the TEG absorption tower is depressurized by a TEG circulating pump, enters a rich liquid heat exchange coil for heat exchange, then enters a TEG flash tank for flash evaporation, and the flash evaporation gas obtained by flash evaporation is used as stripping gas in a TEG fire tube type reboiler; the TEG rich liquid after flash evaporation enters a TEG solution filter to remove mechanical impurities and degradation products in the solution, and enters a rich liquid rectifying column through a lean liquid buffer tank after heat exchange of a lean/rich liquid heat exchanger; the stripping gas is inserted into TEG lean liquor of a TEG fire tube type reboiler to be contacted with TEG rich liquor in a rich liquor rectifying column, the TEG rich liquor is concentrated in the rich liquor rectifying column, then enters the fire tube type reboiler to be heated to about 202 ℃, enters a lean/rich liquor heat exchanger through a lean liquor rectifying column and a lean liquor buffer tank to exchange heat, is pumped to a dry gas/lean liquor heat exchanger through a TEG circulating pump, and enters the top of a TEG absorption tower after cooling and heat exchange;
3. recycling flash gas, stripping gas, waste gas and fuel gas for combustion:
One path of product gas from the tube side of the dry gas/lean liquid heat exchanger is normally output, and the other path of product gas is used as consumed fuel gas in the device through pressure regulation to the flash tank;
4. recovery and recycling of TEG waste liquid:
and after the TEG waste liquid collected from the system enters a solution recovery pipeline, the TEG waste liquid is connected to an inlet of a TEG supplementing pump, is pumped into a TEG supplementing tank through the TEG supplementing pump for storage, and is pumped back into a fire tube type reboiler through the TEG supplementing pump for recycling after being stored to a certain liquid level.
Compared with the prior art, the invention has the following positive effects:
The TEG flash tank is also used as a fuel gas tank, and flash gas is used as stripping gas for a regeneration system; waste gas at the top of the TEG regeneration tower directly enters a fire tube type reboiler of a regeneration system to burn instead of fuel gas, and the waste gas at the top of the regeneration tower is recycled, so that the purposes of energy conservation and emission reduction are achieved; the waste liquid recovery process is improved, the waste liquid recovery tank is arranged above the ground, skid-mounted integration is facilitated, and the waste liquid recovery tank is easy to move and has important significance for single-well test production, shale gas dewatering stations and other projects.
The invention optimizes and improves the TEG flow, not only makes the process simpler and is more beneficial to highly integrated design and easy to move, but also saves energy and reduces emission to a great extent, reduces the operation cost and reduces the one-time investment, and is concretely represented as follows:
(1) A gas supplementing pipeline which is arranged from a product gas pipeline to a flash tank is used as a fuel gas tank by using the TEG flash tank, and flash gas is used as stripping gas for a regeneration system; the fuel gas tank does not need to be arranged independently, so that the flow is simplified, the fuel gas utilization is realized in the device, and the device is more economical and reliable;
(2) Waste gas at the top of the TEG regeneration tower directly enters a fire tube type reboiler of the regeneration system to burn instead of fuel, thereby not only saving waste gas burning facilities and reducing waste gas emission, but also recycling the waste gas at the top of the regeneration tower to achieve the purposes of energy conservation and emission reduction, and simultaneously reducing the disposable investment and operation cost of the whole TEG dehydration device.
(3) The TEG waste liquid recovery process is improved, the waste liquid recovery tank is arranged above the ground, skid-mounted integration is facilitated, occupied space is saved, the skid-mounted waste liquid recovery tank is easy to move, and great convenience is provided for single-well test production, shale gas dewatering stations and other projects. In addition, the bidirectional conveying of the TEG supplementary pump can be realized through the arrangement of the flow, and the operation is convenient.
Drawings
The invention will now be described by way of example and with reference to the accompanying drawings in which:
FIG. 1 is a flow chart of an integrated TEG dehydration integration process of the invention.
Detailed Description
An integrated TEG dehydration integrated process apparatus, as shown in fig. 1, comprising: a raw gas filtering separator 1, a TEG absorption tower 2, a dry gas/lean solution heat exchanger 3, a flash tank 4, a TEG solution filter 5, a TEG circulating pump 6, a lean/rich solution heat exchanger 7, a rich solution heat exchange coil 8, a rich solution rectifying column 9, a fire tube type reboiler 10, a lean solution rectifying column 11, a lean solution buffer tank 12, a TEG supplementing tank 13, a TEG supplementing pump 14, a product gas pressure regulating valve 15, a fuel gas supplementing gas pipeline regulating valve 16, a flash gas pipeline pressure/temperature cascade control regulating valve 17, a flash tank liquid level regulating valve 18, an exhaust gas liquid separating tank 19 and the like, wherein:
The inlet of the TEG absorption tower 2 is connected with the feed gas filtering separator 1, the gas phase outlet of the top of the TEG absorption tower 2 is connected with the tube side of the dry gas/lean liquid heat exchanger 3, and the bottom liquid of the TEG absorption tower 2 is connected with the TEG circulating pump 6; the rich liquid at the outlet of the TEG circulating pump 6 is sequentially connected with a rich liquid heat exchange coil 8, a flash tank 4, a TEG solution filter 5, a lean/rich liquid heat exchanger 7, a lean liquid buffer tank 12 and a rich liquid rectifying column 9; the flash gas outlet of the flash tank 4 is connected with a TEG fire tube type reboiler 10; the rich liquid rectifying column 9 is connected with the fire tube type reboiler 10, the lean liquid rectifying column 11 and the lean liquid buffer tank 12; the outlet of the lean solution buffer tank 12, the lean/rich solution heat exchanger 7, the TEG circulating pump 6, the shell side of the dry gas/lean solution heat exchanger 3 and the liquid phase inlet at the top of the TEG absorption tower 2 are connected in sequence; the top outlet of the rich liquid heat exchange coil 8, the waste gas separating tank 19 and the combustion gas inlet of the fire tube type reboiler 10 are sequentially connected; waste liquid in the lean solution buffer tank 12 and the waste gas separating tank 19 both enter a solution recovery pipeline; the inlet of the TEG-replenishing pump 14 is connected to the solution recovery line and the outlet line at the bottom of the TEG-replenishing tank 13, and the outlet of the TEG-replenishing pump is connected to the TEG-replenishing tank 13 and the fire-tube reboiler 10.
A product gas pressure regulating valve 15 is arranged on a dry gas pipeline of a tube side outlet of the dry gas/lean liquid heat exchanger 3; a fuel gas make-up line regulator valve 16 is provided in the make-up line from the dry gas line to the flash gas line at the outlet of the flash tank 4. A flash tank liquid level regulating valve 18 is provided on the rich liquid outlet line of the bottom outlet of the TEG solution filter 5. A flash gas pipeline pressure/temperature cascade control regulating valve 17 is arranged on a gas phase outlet pipeline at the top of the flash tank 4 and is used for performing cascade interlock control regulation on the temperature of the fire tube type reboiler 10 and the fuel gas pressure for combustion.
The invention also provides an integrated TEG dehydration integrated process method, which comprises the following steps:
step one, the raw natural gas enters a filtering separator 1 to remove mechanical impurities carried in the raw gas, and then enters a separation section at the lower part of a TEG absorption tower 2. And (3) carrying out countercurrent contact on wet natural gas in the tower and TEG lean liquid from bottom to top to remove saturated water in the natural gas. The product gas after the water removal is used as product gas to be output after heat exchange with the lean TEG solution through the dry gas/lean liquid heat exchanger 3, and the pressure of the TEG absorption tower 2 is controlled by the regulating valve 15.
Step two, the TEG rich liquid coming out from the lower part of the TEG absorption tower 2 is depressurized by a TEG circulating pump 6, exchanges heat by a rich liquid heat exchange coil 8 at the top of a rich liquid rectifying column 9, then enters a TEG flash tank 4 for flash evaporation, and the flash evaporation gas obtained by flash evaporation is taken as stripping gas in a TEG fire tube type reboiler 10. The mechanical impurities and degradation products in the solution are removed from the flashed TEG rich solution through a TEG solution filter 5, and the solution enters a rich solution rectifying column 9 through a lean solution buffer tank 12 after heat exchange of a lean/rich solution heat exchanger 7. The stripping gas is inserted into TEG lean liquor of a TEG fire tube type reboiler 10 to contact with TEG rich liquor in a rich liquor rectifying column 9, the TEG rich liquor is concentrated in the rich liquor rectifying column 9, then enters the fire tube type reboiler 10 to be heated to about 202 ℃, enters a lean/rich liquor heat exchanger 7 through a lean liquor rectifying column 11 and a lean liquor buffer tank 12 to exchange heat, and then enters a TEG circulating pump 6 (the pump is an energy recovery pump to convert energy of the rich liquor to boost pressure of the lean liquor) to a dry gas/lean liquor heat exchanger 3, and enters the top of a TEG absorption tower 2 after cooling and heat exchange to complete the TEG absorption and regeneration circulation process.
And thirdly, normally conveying one path of product gas from the tube side of the dry gas/lean liquid heat exchanger 3, and regulating the other path of product gas to the flash tank 4 to be used as fuel gas, stripping gas and the like in the device to consume the fuel gas. The pressure of the flash tank 4, i.e. the fuel gas system, is ensured to be stable by the control of the regulating valve 16. The temperature of the fire tube type reboiler 10 is controlled to be about 202 ℃ by the regulating valve 17, and meanwhile, the amount of exhaust gas combusted by the fire tube type reboiler is controlled, and the matching of the stripping gas amount and the fuel gas amount for combustion is ensured by cascade regulation control of pressure and temperature, so that the quality of lean TEG and the stable operation of a regeneration system are ensured.
Step four, after the TEG waste liquid collected from the system enters a solution recovery pipeline, the TEG waste liquid is connected to the inlet of a TEG supplementing pump 14 through the solution recovery pipeline, is sent into a TEG supplementing tank 13 through the TEG supplementing pump 14 for storage, and is pumped back into a fire tube type reboiler 10 through the TEG supplementing pump 14 for recycling after being stored to a certain liquid level.
The working principle of the invention is as follows: the invention mainly comprises four parts, wherein the first part is an absorption heat exchange and output part of wet purified gas, the second part is a TEG solution circulation part, the flash evaporation, filtration, heat exchange and regeneration of rich liquid and the heat exchange and circulation reinjection of lean liquid are included, the third part is a recycling flow of flash vapor, stripping gas, waste gas and fuel gas for combustion, and the fourth part is the recovery and recovery of TEG waste liquid. The raw natural gas enters a filtering separator to remove mechanical impurities carried in the raw gas, and then enters a separation section at the lower part of the TEG absorption tower. And (3) carrying out countercurrent contact on wet natural gas in the tower and TEG lean liquid from bottom to top to remove saturated water in the natural gas. The product gas after moisture removal is subjected to heat exchange with the lean TEG solution through a dry gas/lean liquid heat exchanger and then is output as the product gas, which is the traditional TEG absorption process principle of the first part.
The TEG rich liquid from the lower part of the TEG absorption tower is depressurized by a TEG circulating pump (energy recovery pump) and is converted into the energy of TEG lean liquid, then heat exchange flash evaporation is sequentially carried out, the flash evaporation TEG rich liquid is subjected to TEG solution filter to remove mechanical impurities and degradation products in the solution, and the solution is subjected to heat exchange with the hot lean liquid by a lean/rich liquid heat exchanger and then enters a rich liquid rectifying column for regeneration concentration. The stripping gas is inserted into TEG lean solution to be in countercurrent contact with TEG rich solution in a rich solution rectifying column, the TEG rich solution is concentrated, then is subjected to heat exchange through a lean solution buffer tank and a lean/rich solution heat exchanger, is pressurized by a TEG circulating pump and is sent to a dry gas/lean solution heat exchanger, and after cooling and heat exchange, the TEG rich solution enters the top of a TEG absorption tower, so that the absorption and regeneration circulation process of the TEG is completed.
One way of air supplementing pipeline is led to the TEG flash tank from the product gas pipeline, the TEG flash tank is also used as a fuel gas tank, flash steam at the top of the flash tank is led into a regeneration system to be used as stripping gas, and regenerated waste gas enters the TEG fire tube type reboiler 10 to be used as combustion gas after being separated by the waste gas separating liquid tank 19. And a regulating valve for cascade linkage control of the temperature of the fire tube type reboiler and the pressure of fuel gas for combustion is arranged on a gas phase outlet pipeline at the top of the flash tank, and the matching of the stripping gas quantity and the fuel gas quantity for combustion is ensured through cascade regulation control of the pressure and the temperature, so that the quality of lean TEG and the stable operation of a regeneration system are ensured.
After the TEG waste liquid collected from the system enters a solution recovery pipeline, the TEG waste liquid is pumped into a TEG supplementing tank for storage through a TEG supplementing pump, and after the TEG waste liquid is stored to a certain liquid level, the TEG waste liquid is pumped back into a fire tube type reboiler for recycling through the TEG supplementing pump, and the bidirectional conveying of the TEG supplementing pump can be realized through the arrangement of the flow.
The invention is improved on the basis of the traditional TEG dehydration process, not only can reduce the production energy consumption, but also can reduce the equipment one-time investment and the pollutant discharge amount, and simultaneously improves the integration of the device, so that the TEG dehydration process is developed towards the directions of high efficiency, energy conservation, environmental protection and integration.
Claims (6)
1. An integrated TEG dehydration integrated process device which is characterized in that: comprises a raw material gas filtering separator, a TEG absorption tower and a dry gas/lean liquid heat exchanger which are connected in sequence; a liquid phase outlet at the bottom of the TEG absorption tower is connected with a TEG circulating pump; the rich liquid outlet of the TEG circulating pump is sequentially connected with a rich liquid heat exchange coil, a flash tank, a TEG solution filter, a lean/rich liquid heat exchanger, a lean liquid buffer tank and a rich liquid rectifying column; the flash gas outlet of the flash tank is connected with a TEG fire tube type reboiler; the rich liquid rectifying column is connected with the fire tube type reboiler, the lean liquid rectifying column and the lean liquid buffer tank; the lean solution buffer tank outlet, the lean/rich solution heat exchanger, the TEG circulating pump, the dry gas/lean solution heat exchanger shell side and the TEG absorption tower top liquid phase inlet are sequentially connected; a fuel gas supplementing pipeline regulating valve is arranged on a supplementing pipeline from a dry gas pipeline at a tube side outlet of the dry gas/lean liquid heat exchanger to a flash evaporation gas pipeline at an outlet of the flash evaporation tank, and a fire tube type reboiler temperature and fuel gas pressure cascade linkage control regulating valve for combustion is arranged on a gas phase outlet pipeline at the top of the flash evaporation tank; the inlet of the TEG supplementing pump is connected with the solution recovery pipeline and the outlet pipeline at the bottom of the TEG supplementing tank, and the outlet of the TEG supplementing pump is connected with the TEG supplementing tank and the fire tube type reboiler respectively.
2. The integrated TEG dehydration process apparatus of claim 1, wherein: the top outlet of the rich liquid heat exchange coil, the waste gas separating tank and the combustion gas inlet of the fire tube type reboiler are sequentially connected.
3. The integrated TEG dehydration process apparatus of claim 1, wherein: and a product gas pressure regulating valve is arranged on a dry gas pipeline at the tube side outlet of the dry gas/lean liquid heat exchanger.
4. The integrated TEG dehydration process apparatus of claim 1, wherein: and a flash tank liquid level regulating valve is arranged on a rich liquid outlet pipeline of the outlet at the bottom of the TEG solution filter.
5. An integrated TEG dehydration integrated process method is characterized in that:
the method comprises the following steps:
1. Absorption heat exchange and output of wet purified gas:
The method comprises the steps that raw natural gas enters a filtering separator to remove mechanical impurities carried in the raw gas, then enters the lower part of a TEG absorption tower, and is in countercurrent contact with TEG lean solution from bottom to top in the tower, saturated water in the natural gas is removed, and product gas after moisture removal enters a dry gas/lean solution heat exchanger to exchange heat with the lean TEG solution and then is output as product gas;
2. TEG solution circulation comprises flash evaporation, filtration, heat exchange and regeneration of rich solution, heat exchange and circulation reinjection of lean solution:
the TEG rich liquid from the lower part of the TEG absorption tower is depressurized by a TEG circulating pump, enters a rich liquid heat exchange coil for heat exchange, then enters a TEG flash tank for flash evaporation, and the flash evaporation gas obtained by flash evaporation is used as stripping gas in a TEG fire tube type reboiler; the TEG rich liquid after flash evaporation enters a TEG solution filter to remove mechanical impurities and degradation products in the solution, and enters a rich liquid rectifying column through a lean liquid buffer tank after heat exchange of a lean/rich liquid heat exchanger; the stripping gas is inserted into TEG lean liquor of a TEG fire tube type reboiler to be contacted with TEG rich liquor in a rich liquor rectifying column, the TEG rich liquor is concentrated in the rich liquor rectifying column, then enters the fire tube type reboiler to be heated to about 202 ℃, enters a lean/rich liquor heat exchanger through a lean liquor rectifying column and a lean liquor buffer tank to exchange heat, is pumped to a dry gas/lean liquor heat exchanger through a TEG circulating pump, and enters the top of a TEG absorption tower after cooling and heat exchange;
3. recycling flash gas, stripping gas, waste gas and fuel gas for combustion:
One path of product gas from the tube side of the dry gas/lean liquid heat exchanger is normally output, and the other path of product gas is used as consumed fuel gas in the device through pressure regulation to the flash tank;
4. recovery and recycling of TEG waste liquid:
and after the TEG waste liquid collected from the system enters a solution recovery pipeline, the TEG waste liquid is connected to an inlet of a TEG supplementing pump, is pumped into a TEG supplementing tank through the TEG supplementing pump for storage, and is pumped back into a fire tube type reboiler through the TEG supplementing pump for recycling after being stored to a certain liquid level.
6. The integrated TEG dehydration process of claim 5, wherein the integrated TEG dehydration process comprises: the pressure of the TEG absorption tower is controlled by a product air pressure regulating valve, and the pressure of the flash tank fuel gas system is stably controlled by a fuel gas supplementing pipeline regulating valve; the pressure/temperature cascade control regulating valve of the flash evaporation gas pipeline controls the temperature of the fire tube type reboiler to be about 202 ℃, and simultaneously controls the amount of waste gas combusted by the fire tube type reboiler, so that the matching of the stripping gas amount and the fuel gas amount for combustion is ensured.
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| CN110018278A (en) * | 2019-04-24 | 2019-07-16 | 重庆科技学院 | Triethylene glycol dehydration and regenerative analogue experimental system based on medium circulation |
| CN112391216A (en) * | 2019-08-15 | 2021-02-23 | 中国石化工程建设有限公司 | Device and method for regenerating triethylene glycol solvent |
| CN111732981B (en) * | 2020-06-10 | 2021-06-08 | 中国石油天然气集团有限公司 | Flash evaporation gas decarburization dehydration method and device based on membrane separation |
| CN114191836A (en) * | 2020-09-02 | 2022-03-18 | 中国石油天然气股份有限公司 | Triethylene glycol dewatering device and natural gas dewatering system |
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