CN113797719A - Skid-mounted LNG deacidification device and method - Google Patents

Skid-mounted LNG deacidification device and method Download PDF

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CN113797719A
CN113797719A CN202111175513.2A CN202111175513A CN113797719A CN 113797719 A CN113797719 A CN 113797719A CN 202111175513 A CN202111175513 A CN 202111175513A CN 113797719 A CN113797719 A CN 113797719A
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amine
chamber
lean
liquid
combined
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文向南
蔡以勇
王元宏
陈丽英
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Chengdu Shenleng Liquefaction Plant Co ltd
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Chengdu Shenleng Liquefaction Plant Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
    • B01D29/50—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition
    • B01D29/56—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with multiple filtering elements, characterised by their mutual disposition in series connection
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D35/00—Filtering devices having features not specifically covered by groups B01D24/00 - B01D33/00, or for applications not specifically covered by groups B01D24/00 - B01D33/00; Auxiliary devices for filtration; Filter housing constructions
    • B01D35/02—Filters adapted for location in special places, e.g. pipe-lines, pumps, stop-cocks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • 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
    • B01D53/1456—Removing acid components
    • 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
    • C10L3/102—Removal of contaminants of acid contaminants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
    • F25D1/00—Devices using naturally cold air or cold water
    • F25D1/02—Devices using naturally cold air or cold water using naturally cold water, e.g. household tap water
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
    • F25D17/00—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces
    • F25D17/02—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces for circulating liquids, e.g. brine

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Abstract

The invention discloses a skid-mounted LNG deacidification device and a skid-mounted LNG deacidification method, and solves the technical problems that a deacidification device in the prior art is complex in structure, high in production configuration cost and difficult to maintain and overhaul in the later period of equipment. The combined absorption tower comprises a combined absorption tower (100), a combined regeneration tower (200), a lean and rich amine heat exchanger (313), a lean amine cooler (304), an amine storage tank (300) and a lean amine pump (302), wherein the combined absorption tower (100) is sequentially provided with a cooling chamber I (103), a separation chamber I (102) and an absorption chamber (101) from top to bottom, and the top end of the absorption chamber (101) is also provided with a liquid distributor I (115). According to the skid-mounted LNG deacidification device and method provided by the invention, the number of equipment, pipelines and valves is reduced by combining the skid-mounted or modularized deacidification device and equipment, so that the investment of a deacidification system is reduced, and the same deacidification effect and purification index can be achieved.

Description

Skid-mounted LNG deacidification device and method
Technical Field
The invention belongs to the technical field of energy, and particularly relates to a skid-mounted LNG deacidification device and method.
Background
The main component of natural gas is methane, and after the natural gas is fully combusted, only carbon dioxide and water molecules are generated, so that the natural gas is known as the cleanest fossil energy on the earth. Liquefied Natural Gas (LNG) is a liquid obtained by purifying, cooling, supercooling Natural Gas to-162 ℃, and condensing the Natural Gas in a low-temperature storage tank of 0.1 MPa. The LNG obtained by treatment has the advantages of no color, no odor, no toxicity and no corrosiveness, the volume of the LNG is about 1/625 of the volume of the same amount of gaseous natural gas, the mass of the liquefied natural gas is only about 45% of the water with the same volume, and the storage space of energy is greatly saved.
Before the natural gas is liquefied at low temperature to obtain LNG, the natural gas produced by a gas field needs to be purified to remove corrosive and low-temperature solidified impurities in the natural gas produced by the gas field, and the impurities mainly comprise three parts, namely deacidification, dehydration and demercuration, wherein the deacidification part is an important concern about energy consumption, equipment protection and safe production in the purification process of the LNG production.
In the prior art, the deacidification technology widely applied to the field of natural gas treatment and processing is an MDEA absorption technology, and the MDEA deacidification technology is used for dissolving acid gas in gas at normal temperature by using MDEA water solution and desorbing the acid gas under the conditions of high temperature and low pressure, so that the acid gas in the natural gas is removed, equipment is prevented from being corroded in the storage process of LNG, and the safety of LNG in storage is maintained.
In the prior patents, patent application No. CN200810044270.7, patent application No. CN201520326787.0, patent application No. CN201620389925.4, patent application No. CN202010558598.1, patent application No. an energy-saving natural gas MDEA decarbonization system and decarbonization process thereof, patent application No. CN202011171092.1, patent application No. an energy-saving natural gas MDEA decarbonization device and method thereof, patent application No. CN202021764682.0, patent application No. an MDEA solvent-based LNG decarbonization system, all patents in the above patents adopt MDEA absorption method to remove acid gas in LNG, but the devices adopted in the above patents all have many defects of complicated equipment and system, and are not beneficial to the operation of the devices in the subsequent use, and subsequent troubleshooting and troubleshooting are difficult.
Disclosure of Invention
The invention aims to provide a skid-mounted LNG deacidification device and a skid-mounted LNG deacidification method, and the technical problems that in the prior art, the structure of a deacidification device is complex, the production and configuration costs are high, and the later maintenance and overhaul of equipment are difficult are solved.
In order to achieve the purpose, the invention provides the following technical scheme:
the invention provides a skid-mounted LNG deacidification device which comprises a combined absorption tower, a combined regeneration tower, a lean and rich amine heat exchanger, a lean amine cooler, an amine storage tank and a lean amine pump, wherein the combined absorption tower is connected with the combined regeneration tower;
the combined absorption tower is sequentially provided with a first cooling chamber, a first separation chamber and an absorption chamber from top to bottom, the top end of the absorption chamber is also provided with a first liquid distributor, the absorption chamber is connected with the first cooling chamber through a first steam pipeline, the first cooling chamber is connected with the first separation chamber through a channel of a cooling pipe, and the bottom of the first separation chamber is provided with a first liquid flooding pipe connected with the first liquid distributor; the bottom end of the absorption chamber of the combined absorption tower is provided with a natural gas inlet pipe for entering natural gas to be treated and a tower bottom outlet pipe for discharging rich amine solution, the first liquid distributor is also provided with a lean amine liquid inlet pipe for entering lean amine solution, and the first separation chamber is provided with a natural gas outlet pipe for discharging deacidified natural gas;
the combined regeneration tower is sequentially provided with a second cooling chamber, a second analysis chamber, a second separation chamber and a reboiler from top to bottom, the top end of the second analysis chamber is also provided with a second liquid distributor, the second analysis chamber is connected with the second cooling chamber through a second steam pipeline, the second cooling chamber is connected with the second separation chamber through a channel of a cooling pipe, and the bottom of the second separation chamber is provided with a second liquid flooding pipe connected with the second liquid distributor; the reboiler is provided with a lean amine outlet pipe for outputting the treated lean amine solution, the second separation chamber is also connected with an acid gas outlet pipe for outputting acid-containing gas, and the second liquid distributor is also connected with an rich amine inlet pipe for entering rich amine gas;
the tower bottom outlet pipe is connected with the rich amine inlet pipe, and a lean rich amine heat exchanger is also arranged on a connecting pipeline of the tower bottom outlet pipe and the rich amine inlet pipe; the lean amine outlet pipe is connected with the amine storage tank, and a lean rich amine heat exchanger is also arranged on a connecting pipeline of the lean amine outlet pipe and the amine storage tank; the amine storage tank is connected with the lean amine liquid inlet pipe, and a lean amine pump and a lean amine cooler are further arranged on a connecting pipeline of the amine storage tank and the lean amine liquid inlet pipe;
a cold source inlet pipe and a cold source outlet pipe are respectively arranged on the cooling chamber I, the cooling chamber II and the lean amine cooler; a heat source inlet pipe and a heat source outlet pipe are arranged on the reboiler; the amine storage tank is also provided with a first nitrogen inlet pipe for nitrogen to enter and a chemical inlet pipe for chemicals to enter; and a second nitrogen inlet pipe for introducing nitrogen is also arranged on the second separation chamber.
Optionally or preferably, a first reflux liquid-flooding pipe connected with the first separation chamber and the bottom end of the combined absorption tower is further arranged outside the combined absorption tower; and a second reflux liquid-flooding pipe connected with the second separation chamber and the bottom end of the combined regeneration tower is also arranged outside the combined regeneration tower.
Optionally or preferably, a return pipeline connected with the amine storage tank is further arranged at the outlet pipe end of the lean amine cooler, and a pipeline filter I, a lean amine filter and a pipeline filter II are sequentially arranged on the return pipeline along the flow direction of the lean amine.
Optionally or preferably, the cold source inlet pipe and the heat source inlet pipe are respectively provided with a control valve for the inlet and outlet of the heat source and the cold source; a control valve and a double check valve are arranged on a connecting pipeline of the lean amine cooler and the first liquid distributor; the return pipeline is also provided with a control valve; the nitrogen inlet pipe I and the nitrogen inlet pipe II are respectively provided with a control valve; and the tower bottom pipeline is also provided with a liquid level control valve and a low liquid level stop valve.
Optionally or preferably, the absorption chamber of the absorption tower is a packed tower;
the reboiler adopts any one of a kettle reboiler, a thermosyphon reboiler, a forced circulation reboiler and a built-in reboiler, and the heat source of the reboiler is any one of a power supply, heat conducting oil and natural gas;
the cold source of the first cooling chamber, the second cooling chamber and the lean amine cooler can be any one of circulating cooling water, circulating chilled water, propane, refrigerant and low-temperature raw natural gas.
Optionally or preferably, the first cooling chamber and the first separation chamber of the combined absorption tower are arranged in a combined manner, and the first cooling chamber and the first separation chamber which are arranged in a combined manner can be separately arranged outside the absorption chamber and have the same height as the top of the absorption chamber; the first steam pipeline is communicated with the first cooling chamber and the absorption chamber, and the second flood pipe is connected with the first separation chamber and the bottom of the combined absorption tower.
Optionally or preferably, the second cooling chamber and the second separating chamber of the combined regeneration tower are arranged in a combined manner, and the second cooling chamber and the second separating chamber which are arranged in a combined manner can be separately arranged outside the absorption chamber and have the same height as the top of the absorption chamber; and the second steam pipeline is communicated with the second cooling chamber and the absorption chamber, and the second liquid flooding pipe is connected with the second separation chamber and the bottom of the combined regeneration tower.
The invention provides a deacidification method of a skid-mounted LNG deacidification device, which comprises the following steps:
a. inputting raw natural gas to be deacidified into a combined absorption tower, contacting with a descending amine liquid in an absorption chamber, enabling the deacidified natural gas entering the top of the absorption chamber of the absorption tower to enter a cooling chamber I through a steam pipeline I to be cooled by a cold source, separating condensed water in a separation chamber I, finally enabling the deacidified natural gas to leave the combined absorption tower through a natural gas outlet pipe, and enabling the condensed water in the separation chamber I to enter a liquid distributor I along a liquid flooding pipe I;
b. the rich amine liquid absorbing the acid gas enters a lean rich amine heat exchanger from a tower bottom outlet pipe of the combined absorption tower, the rich amine liquid is heated to 90-105 ℃ and then enters a liquid distributor II of the combined regeneration tower along a rich amine inlet pipe, the rich amine liquid is contacted with rising water vapor from top to bottom in the desorption chamber, the amine liquid is heated again after entering a reboiler to be regenerated into lean amine liquid, the acid gas at the top of the desorption chamber enters a cooling chamber II along a steam pipeline II to be condensed, condensed water is separated in a separation chamber II, finally the acid gas leaves the combined regeneration tower through an acid gas outlet pipe, and the condensed water in the separation chamber II enters the liquid distributor II along a flooding pipe II;
c. the lean amine liquid regenerated in the combined regeneration tower enters a lean rich amine heat exchanger along a lean amine outlet pipe, is cooled to 55-75 ℃ in the lean rich amine heat exchanger, and then enters an amine storage tank; and after entering a lean amine pump, the lean amine in the amine storage tank is pressurized and then enters a lean amine cooler to be cooled by a cold source, and the cooled lean amine liquid enters a liquid distributor I of the combined absorption tower, so that the circulation of the amine liquid is completed.
Optionally or preferably, the steps further comprise: and c, allowing 75-90% of the lean amine liquid cooled by the lean amine cooler in the step c to enter a first liquid distributor of the combined absorption tower, and allowing 10-25% of the cooled lean amine liquid to pass through a first pipeline filter, a lean amine filter and a second pipeline filter in sequence along a backflow pipeline and return to the amine storage tank.
Optionally or preferably, the pressure of the raw natural gas to be deacidified is 0.5-10.0 MPa, the temperature is 5-55 ℃, and the pressure of the raw natural gas to be deacidified also comprises various hydrocarbon gases rich in methane.
Based on the technical scheme, the embodiment of the invention can at least produce the following technical effects:
the skid-mounted LNG deacidification device and the method provided by the invention provide a conveniently skid-mounted or modularized deacidification gas device, and gaseous water in acid gas is condensed and then recovered to the lower end of a tower body through the cooling chamber and the separation chamber arranged at the tops of the combined regeneration tower and the combined absorption tower, so that the arrangement of a reflux pump is avoided, the acid gas recovery cost is reduced, the number of equipment, pipelines and valves is reduced due to the arrangement of the combined absorption tower and the combined regeneration tower, the investment of a deacidification gas system is reduced, and the same deacidification gas effect and purification index can be achieved.
Drawings
FIG. 1 is a schematic structural view of embodiment 1 of the present invention;
FIG. 2 is a schematic structural view of embodiment 2 of the present invention;
fig. 3 is a schematic structural diagram of embodiment 3 of the present invention.
In the figure: 100. a combined absorption tower; 101. an absorption chamber; 102. a first separation chamber; 103. a first cooling chamber; 104. a first backflow liquid-flooding pipe; 111. natural gas inlet pipe; 112. a first steam pipeline; 113. a natural gas outlet pipe; 114. a flooding pipe I; 115. a first liquid distributor; 200. a combined regeneration tower; 201. an analysis chamber; 202. a second separation chamber; 203. a second cooling chamber; 204. a second liquid distributor; 205. a flooding pipe II; 300. an amine storage tank; 302. a lean amine pump; 304. a lean amine cooler; 307. a double check valve; 308. a lean amine liquid inlet pipe; 309. a tower bottom outlet pipe; 310. a liquid level control valve; 311. a low liquid level shut-off valve; 313. a lean rich amine heat exchanger; 314. a rich amine inlet pipe; 315. a reboiler; 316. a lean amine outlet pipe; 321. a return line; 323. a first pipeline filter; 324. a lean amine filter; 325. a second pipeline filter; 332. a nitrogen inlet pipe I; 333. chemical inlet pipe; 361. a nitrogen inlet pipe II; 371. a second steam pipeline; 372. an acid gas outlet pipe; 374. and a second backflow liquid-flooding pipe.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be described in detail below. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the examples given herein without any inventive step, are within the scope of the present invention.
Example 1
As shown in fig. 1:
the invention provides a skid-mounted LNG deacidification device, which comprises a combined absorption tower 100, a combined regeneration tower 200, a lean and rich amine heat exchanger 313, a lean amine cooler 304, an amine storage tank 300 and a lean amine pump 302, wherein the lean amine pump is connected with the combined regeneration tower 200;
the combined absorption tower 100 is sequentially provided with a first cooling chamber 103, a first separation chamber 102 and an absorption chamber 101 from top to bottom, the top end of the absorption chamber 101 is further provided with a first liquid distributor 115, the absorption chamber 101 is connected with the first cooling chamber 103 through a first steam pipeline 112, the first cooling chamber 103 is connected with the first separation chamber 102 through a cooling pipe channel, and the bottom of the first separation chamber 102 is provided with a first liquid flooding pipe 114 connected with the first liquid distributor 115; a natural gas inlet pipe 111 for entering natural gas to be treated and a tower bottom outlet pipe 309 for discharging rich amine solution are arranged at the bottom end of an absorption chamber 101 of the combined absorption tower 100, a lean amine liquid inlet pipe 308 for entering lean amine solution is further arranged on the first liquid distributor 115, and a natural gas outlet pipe 113 for discharging deacidified natural gas is arranged on the first separation chamber 102;
the combined regeneration tower 200 is sequentially provided with a second cooling chamber 203, a second analysis chamber 201, a second separation chamber 202 and a reboiler 315 from top to bottom, the top end of the second analysis chamber 201 is also provided with a second liquid distributor 204, the second analysis chamber 201 is connected with the second cooling chamber 203 through a second steam pipeline 371, the second cooling chamber 203 is connected with the second separation chamber 202 through a channel of a cooling pipe, and the bottom of the second separation chamber 202 is provided with a second liquid flooding pipe 205 connected with the second liquid distributor 204; a lean amine outlet pipe 316 for outputting the treated lean amine solution is arranged on the reboiler 315, an acid gas outlet pipe 372 for outputting acid-containing gas is further connected to the second separation chamber 202, and an rich amine inlet pipe 314 for allowing rich amine gas to enter is further connected to the second liquid distributor 204;
the tower bottom outlet pipe 309 is connected with the rich amine inlet pipe 314, and a lean rich amine heat exchanger 313 is further arranged on a connecting pipeline of the tower bottom outlet pipe 309 and the rich amine inlet pipe 314; the lean amine outlet pipe 316 is connected with the amine storage tank 300, and a lean rich amine heat exchanger 313 is further arranged on a connecting pipeline between the lean amine outlet pipe 316 and the amine storage tank 300; the amine storage tank 300 is connected with a lean amine liquid inlet pipe 308, and a lean amine pump 302 and a lean amine cooler 304 are further arranged on a connecting pipeline of the amine storage tank 300 and the lean amine liquid inlet pipe 308;
a cold source inlet pipe and a cold source outlet pipe are respectively arranged on the first cooling chamber 103, the second cooling chamber 203 and the lean amine cooler 304; a heat source inlet pipe and a heat source outlet pipe are arranged on the reboiler 315; the amine storage tank 300 is also provided with a first nitrogen inlet pipe 332 for nitrogen to enter and a chemical inlet pipe 333 for chemicals to enter; and a second nitrogen inlet pipe 361 for introducing nitrogen is also arranged on the second separation chamber 202.
In the device, in use, acid gas is transferred from natural gas to an amine solution in the absorption chamber 101 of the combined absorption tower 100 to generate a natural gas product and an amine-rich solution; the rich amine liquid contacts with the rising steam from top to bottom in the desorption chamber 201 of the combined regeneration tower 200, the acid substances are desorbed into the steam, and the rich amine liquid falls into the reboiler 315, so that the lean amine liquid is regenerated and returns to the combined absorption tower. The mole ratio content indexes of the acid gas in the deacidified natural gas are as follows: CO 2220 to 100ppm of H2S≤4ppm。
As an alternative embodiment, the outside of the combined absorption tower 100 is also provided with a reflux liquid-flooding pipe 104 which is connected with the separation chamber I102 and the bottom end of the combined absorption tower 100; and a second reflux liquid-flooding pipe 374 connecting the second separation chamber 202 and the bottom end of the combined regeneration tower 200 is also arranged outside the combined regeneration tower 200.
The first return flooding pipe 104 and the second return flooding pipe 374 can help to return excessive solution accumulated in the separation chamber, so that the normal use of the device is maintained, and the flooding phenomenon is avoided.
As an alternative embodiment, the outlet pipe end of the lean amine cooler 304 is further provided with a return pipe 321 connected to the amine storage tank 300, and a first pipe filter 323, a second pipe filter 324 and a second pipe filter 325 are sequentially arranged on the return pipe 321 along the flow direction of the lean amine.
As an optional implementation manner, the cold source inlet pipe and the heat source inlet pipe are respectively provided with a control valve for the inlet and the outlet of the heat source and the cold source; a control valve and a double check valve 307 are arranged on a connecting pipeline of the lean amine cooler 304 and the first liquid distributor 115; a control valve is also arranged on the return pipeline 321; the first nitrogen inlet pipe 332 and the second nitrogen inlet pipe 361 are respectively provided with a control valve; the tower bottom pipeline is also provided with a liquid level control valve 310 and a low liquid level cut-off valve 311.
As an alternative embodiment, the absorption chamber 101 of the combined absorption tower 100 is a packed tower;
the reboiler 315 is any one of a kettle reboiler 315, a thermosiphon reboiler 315, a forced circulation reboiler 315 and a built-in reboiler 315, and a heat source of the reboiler 315 is any one of a power supply, heat conducting oil and natural gas;
the cold source of the cooling chamber one 103, the cooling chamber two 203 and the lean amine cooler 304 can be any one of circulating cooling water, circulating chilled water, propane, refrigerant and low-temperature raw natural gas.
Example 2
As shown in fig. 2:
compared with the embodiment 1, the skid-mounted LNG deacidification device has the advantages that the first cooling chamber 103 and the first separation chamber 102 of the combined absorption tower 100 in the embodiment 2 are combined, and the first cooling chamber 103 and the first separation chamber 102 which are combined can be independently arranged outside the absorption chamber 101 and have the same height as the top of the absorption chamber 101; a first steam pipeline 112 is communicated with the first cooling chamber 103 and the absorption chamber 101, and a first flood pipe 114 is connected with the first separation chamber 102 and the bottom of the combined absorption tower 100.
The second cooling chamber 203 and the second separating chamber 202 of the combined regeneration tower 200 are combined, and the second cooling chamber 203 and the second separating chamber 202 which are combined can be separately arranged outside the absorption chamber 101 and have the same height as the top of the absorption chamber 101; the second steam pipeline 371 is communicated with the second cooling chamber 203 and the absorption chamber 101, and the second flooding pipe 205 is connected with the second separation chamber 202 and the bottom of the combined regeneration tower 200.
Partial components of the combined absorption tower 100 and the combined regeneration tower 200 are disassembled and installed, so that the skid blocks can be conveniently and respectively transported when the transportation length is limited.
Example 3
As shown in fig. 3:
compared with the embodiment 2, in the embodiment 3, the return pipeline 321 and the first pipeline filter 323, the lean amine filter 324 and the second pipeline filter 325 which are sequentially arranged on the return pipeline 321 are arranged on a pipeline between the lean amine cooler 304 and the lean amine liquid inlet pipe 308.
Examples of the experiments
The invention provides a deacidification method of a skid-mounted LNG deacidification device, which comprises the following steps:
a. inputting raw natural gas to be deacidified into a combined absorption tower 100, contacting with a descending amine liquid in an absorption chamber 101, enabling the deacidified natural gas entering the top of the absorption chamber 101 of the absorption tower to enter a cooling chamber 103 through a first steam pipeline 112 to be cooled by a cold source, separating condensed water in a separation chamber 102, enabling the deacidified natural gas to leave the combined absorption tower 100 through a first natural gas outlet pipe 113, and enabling the condensed water in the separation chamber 102 to enter a first liquid distributor 115 along a first flood pipe 114;
b. the rich amine liquid absorbing the acid gas enters a lean rich amine heat exchanger 313 from an outlet pipe 309 at the bottom of the combined absorption tower 100, is heated to 90-105 ℃, and then enters a second liquid distributor 204 of the combined regeneration tower 200 along an amine inlet pipe 314, the rich amine liquid contacts with rising water vapor from top to bottom in the desorption chamber 201, the amine liquid enters a reboiler 315 and is heated again to be regenerated into lean amine liquid, the acid gas at the top of the desorption chamber 201 enters a second cooling chamber 203 along a second steam pipeline 371 for condensation, condensed water is separated in a second separation chamber 202, finally the acid gas leaves the combined regeneration tower 200 through an acid gas outlet pipe 372, and the condensed water in the second separation chamber 202 enters the second liquid distributor 204 along a second flooding pipe 205;
c. the lean amine liquid regenerated in the combined regeneration tower 200 enters a lean rich amine heat exchanger 313 along a lean amine outlet pipe 316, is cooled to 55-75 ℃ in the lean rich amine heat exchanger, and then enters an amine storage tank 300; after entering the lean amine pump 302, the lean amine in the amine storage tank 300 is pressurized, and then enters the lean amine cooler 304 to be cooled by the cold source, and the cooled lean amine liquid enters the first liquid distributor 115 of the combined absorption tower 100, thereby completing the amine liquid circulation.
As an optional implementation, the steps further include: and c, feeding 75-90% of the lean amine liquid cooled by the lean amine cooler 304 in the step c into a first liquid distributor 115 of the combined absorption tower 100, and returning 10-25% of the cooled lean amine liquid to the amine storage tank 300 along a return pipeline 321 through a first pipeline filter 323, a lean amine filter 324 and a second pipeline filter 325 in sequence.
As an optional implementation mode, the pressure of the raw natural gas to be deacidified is 0.5-10.0 MPa, the temperature is 5-55 ℃, and the pressure of the raw natural gas to be deacidified also comprises various hydrocarbon gases rich in methane.
The natural gas system parameters of the acid gas inlet and outlet system in example 1 are shown in table 1:
TABLE 1 Natural gas System parameters
Figure BDA0003295351830000091
The natural gas system parameters of the acid gas inlet and outlet system in example 2 are shown in table 2:
TABLE 2 Natural gas System parameters
Figure BDA0003295351830000092
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention, and all the changes or substitutions should be covered within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.

Claims (10)

1. The utility model provides a sled dress formula LNG deacidification device which characterized in that: comprises a combined absorption tower (100), a combined regeneration tower (200), a lean rich amine heat exchanger (313), a lean amine cooler (304), an amine storage tank (300) and a lean amine pump (302);
the combined absorption tower (100) is sequentially provided with a first cooling chamber (103), a first separation chamber (102) and an absorption chamber (101) from top to bottom, the top end of the absorption chamber (101) is further provided with a first liquid distributor (115), the absorption chamber (101) is connected with the first cooling chamber (103) through a first steam pipeline (112), the first cooling chamber (103) is connected with the first separation chamber (102) through a channel of a cooling pipe, and the bottom of the first separation chamber (102) is provided with a first liquid flooding pipe (114) connected with the first liquid distributor (115); a natural gas inlet pipe (111) for entering natural gas to be treated and a tower bottom outlet pipe (309) for discharging rich amine solution are arranged at the bottom end of an absorption chamber (101) of the combined absorption tower (100), a lean amine liquid inlet pipe (308) for entering lean amine solution is further arranged on the liquid distributor I (115), and a natural gas outlet pipe (113) for discharging deacidified natural gas is arranged on the separation chamber I (102);
the combined regeneration tower (200) is sequentially provided with a second cooling chamber (203), a second analysis chamber (201), a second separation chamber (202) and a reboiler (315) from top to bottom, the top end of the second analysis chamber (201) is also provided with a second liquid distributor (204), the second analysis chamber (201) is connected with the second cooling chamber (203) through a second steam pipeline (371), the second cooling chamber (203) is connected with the second separation chamber (202) through a channel of a cooling pipe, and the bottom of the second separation chamber (202) is provided with a second liquid flooding pipe (205) connected with the second liquid distributor (204); a lean amine outlet pipe (316) for outputting the treated lean amine solution is arranged on the reboiler (315), an acid gas outlet pipe (372) for outputting acid-containing gas is connected to the second separation chamber (202), and a rich amine inlet pipe (314) for entering rich amine gas is connected to the second liquid distributor (204);
the tower bottom outlet pipe (309) is connected with the rich amine inlet pipe (314), and a lean rich amine heat exchanger (313) is further arranged on a connecting pipeline of the tower bottom outlet pipe (309) and the rich amine inlet pipe (314); the lean amine outlet pipe (316) is connected with the amine storage tank (300), and a lean rich amine heat exchanger (313) is further arranged on a connecting pipeline of the lean amine outlet pipe (316) and the amine storage tank (300); the amine storage tank (300) is connected with the lean amine liquid inlet pipe (308), and a lean amine pump (302) and a lean amine cooler (304) are further arranged on a connecting pipeline of the amine storage tank (300) and the lean amine liquid inlet pipe (308);
a cold source inlet pipe and a cold source outlet pipe are respectively arranged on the first cooling chamber (103), the second cooling chamber (203) and the lean amine cooler (304); a heat source inlet pipe and a heat source outlet pipe are arranged on the reboiler (315); the amine storage tank (300) is also provided with a first nitrogen inlet pipe (332) for the inlet of nitrogen and a chemical inlet pipe (333) for the inlet of chemicals; and a second nitrogen inlet pipe (361) for introducing nitrogen is also arranged on the second separation chamber (202).
2. The skid-mounted LNG deacidification apparatus according to claim 1, wherein: the outside of the combined absorption tower (100) is also provided with a first reflux liquid-flooding pipe (104) which is connected with the first separation chamber (102) and the bottom end of the combined absorption tower (100); and a second reflux liquid-flooding pipe (374) which is connected with the second separation chamber (202) and the bottom end of the combined regeneration tower (200) is also arranged outside the combined regeneration tower (200).
3. The skid-mounted LNG deacidification apparatus according to claim 1, wherein: and the outlet pipe end of the lean amine cooler (304) is also provided with a return pipe (321) connected with the amine storage tank (300), and the return pipe (321) is sequentially provided with a first pipe filter (323), a lean amine filter (324) and a second pipe filter (325) along the flow direction of lean amine.
4. The skid-mounted LNG deacidification apparatus according to claim 3, wherein: the cold source inlet pipe and the heat source inlet pipe are respectively provided with a control valve for the inlet and outlet of the heat source and the cold source; a control valve and a double check valve (307) are arranged on a connecting pipeline of the lean amine cooler (304) and the liquid distributor I (115); the return pipeline (321) is also provided with a control valve; control valves are respectively arranged on the first nitrogen inlet pipe (332) and the second nitrogen inlet pipe (361); and a liquid level control valve (310) and a low liquid level stop valve (311) are also arranged on the tower bottom pipeline.
5. The skid-mounted LNG deacidification apparatus according to claim 1, wherein: the absorption chamber (101) of the absorption tower is a packed tower;
the reboiler (315) adopts any one of a kettle type reboiler (315), a thermosiphon type reboiler (315), a forced circulation type reboiler (315) and a built-in reboiler (315), and a heat source of the reboiler (315) is any one of a power supply, heat conduction oil and natural gas;
the cold sources of the cooling chamber I (103), the cooling chamber II (203) and the lean amine cooler (304) can be any one of circulating cooling water, circulating chilled water, propane, refrigerant and low-temperature raw natural gas.
6. The skid-mounted LNG deacidification apparatus according to claim 1, wherein: the first cooling chamber (103) and the first separating chamber (102) of the combined absorption tower (100) are combined, and the first cooling chamber (103) and the first separating chamber (102) which are combined can be separately arranged outside the absorption chamber (101) and have the same height as the top of the absorption chamber (101); the first steam pipeline (112) is communicated with the first cooling chamber (103) and the absorption chamber (101), and the first flooding pipe (114) is connected with the first separation chamber (102) and the bottom of the combined absorption tower (100).
7. The skid-mounted LNG deacidification apparatus according to claim 1, wherein: the second cooling chamber (203) and the second separating chamber (202) of the combined regeneration tower (200) are combined, and the second cooling chamber (203) and the second separating chamber (202) which are combined can be independently arranged outside the absorption chamber (101) and have the same height as the top of the absorption chamber (101); and a second steam pipeline (371) is communicated with the second cooling chamber (203) and the absorption chamber (101), and a second flooding pipe (205) is connected with the second separation chamber (202) and the bottom of the combined regeneration tower (200).
8. The deacidification method of the skid-mounted LNG deacidification apparatus according to any one of claims 1 to 7, comprising the following steps:
a. feeding raw natural gas to be deacidified into a combined absorption tower (100), contacting with descending amine liquid in an absorption chamber (101), feeding the deacidified natural gas entering the top of the absorption chamber (101) of the absorption tower into a cooling chamber I (103) through a steam pipeline I (112), cooling by a cold source, separating condensed water in a separation chamber I (102), finally, allowing the deacidified natural gas to leave the combined absorption tower (100) through a natural gas outlet pipe (113), and allowing the condensed water in the separation chamber I (102) to enter a liquid distributor I (115) along a liquid flooding pipe I (114);
b. the rich amine liquid absorbing the acid gas enters a lean rich amine heat exchanger (313) from a tower bottom outlet pipe (309) of a combined absorption tower (100), the rich amine liquid is heated to 90-105 ℃ and then enters a liquid distributor II (204) of a combined regeneration tower (200) along a rich amine inlet pipe (314), the rich amine liquid contacts with rising water vapor from top to bottom in a desorption chamber (201), the amine liquid enters a reboiler (315) and is heated again to regenerate lean amine liquid, the acid gas on the top of the desorption chamber (201) enters a cooling chamber II (203) along a steam pipeline II (371) to be condensed and is separated into condensed water in a separation chamber II (202), finally the acid gas leaves the combined regeneration tower (200) through an acid gas outlet pipe (372), and the condensed water in the separation chamber II (202) enters the liquid distributor II (204) along a flooding pipe II (205);
c. the lean amine liquid regenerated in the combined regeneration tower (200) enters a lean rich amine heat exchanger (313) along a lean amine outlet pipe (316), is cooled to 55-75 ℃ and then enters an amine storage tank (300); after entering a lean amine pump (302), lean amine in an amine storage tank (300) is pressurized and enters a lean amine cooler (304) to be cooled by a cold source, and cooled lean amine liquid enters a liquid distributor I (115) of the combined absorption tower (100), so that amine liquid circulation is completed.
9. The deacidification method of a skid-mounted LNG deacidification apparatus according to claim 8, wherein said steps further comprise: and c, feeding 75-90% of the lean amine liquid cooled by the lean amine cooler (304) in the step c into a first liquid distributor (115) of the combined absorption tower (100), and returning 10-25% of the cooled lean amine liquid to the amine storage tank (300) along a return pipeline (321) in sequence through a first pipeline filter (323), a lean amine filter (324) and a second pipeline filter (325).
10. The deacidification method of the skid-mounted LNG deacidification device according to claim 8, wherein the deacidification method comprises the following steps: the pressure of the raw material natural gas to be deacidified is 0.5-10.0 MPa, the temperature is 5-55 ℃, and the pressure of the raw material natural gas to be deacidified also comprises various hydrocarbon gases rich in methane.
CN202111175513.2A 2021-10-09 2021-10-09 Skid-mounted LNG deacidification device and method Pending CN113797719A (en)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20160046592A (en) * 2014-10-21 2016-04-29 현대중공업 주식회사 Energy savings type- LNG Feed gas pre-processing apparatus
CN110527572A (en) * 2019-09-11 2019-12-03 张家港富瑞特种装备股份有限公司 A kind of natural gas depickling module
CN216171218U (en) * 2021-10-09 2022-04-05 成都深冷液化设备股份有限公司 Sled dress formula LNG deacidification device

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20160046592A (en) * 2014-10-21 2016-04-29 현대중공업 주식회사 Energy savings type- LNG Feed gas pre-processing apparatus
CN110527572A (en) * 2019-09-11 2019-12-03 张家港富瑞特种装备股份有限公司 A kind of natural gas depickling module
CN216171218U (en) * 2021-10-09 2022-04-05 成都深冷液化设备股份有限公司 Sled dress formula LNG deacidification device

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