CN116445196B - Method and device for efficiently regenerating amine liquid of coupling heat pump - Google Patents
Method and device for efficiently regenerating amine liquid of coupling heat pump Download PDFInfo
- Publication number
- CN116445196B CN116445196B CN202310339391.9A CN202310339391A CN116445196B CN 116445196 B CN116445196 B CN 116445196B CN 202310339391 A CN202310339391 A CN 202310339391A CN 116445196 B CN116445196 B CN 116445196B
- Authority
- CN
- China
- Prior art keywords
- liquid
- amine liquid
- regeneration
- carbon dioxide
- regeneration tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 299
- 150000001412 amines Chemical class 0.000 title claims abstract description 194
- 238000000034 method Methods 0.000 title claims abstract description 42
- 230000001172 regenerating effect Effects 0.000 title claims abstract description 20
- 230000008878 coupling Effects 0.000 title claims abstract description 10
- 238000010168 coupling process Methods 0.000 title claims abstract description 10
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 10
- 238000011069 regeneration method Methods 0.000 claims abstract description 153
- 230000008929 regeneration Effects 0.000 claims abstract description 151
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 148
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 74
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 74
- 238000003795 desorption Methods 0.000 claims abstract description 40
- 238000000926 separation method Methods 0.000 claims abstract description 21
- 238000003303 reheating Methods 0.000 claims description 19
- 230000008569 process Effects 0.000 abstract description 16
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 238000005262 decarbonization Methods 0.000 abstract description 5
- 239000000126 substance Substances 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 14
- 239000002253 acid Substances 0.000 description 10
- 238000010438 heat treatment Methods 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- 239000003345 natural gas Substances 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 230000009471 action Effects 0.000 description 4
- 239000012535 impurity Substances 0.000 description 3
- 239000003949 liquefied natural gas Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 125000001741 organic sulfur group Chemical group 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
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- 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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- B01D2252/204—Amines
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/12—Regeneration of a solvent, catalyst, adsorbent or any other component used to treat or prepare a fuel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to the technical field of energy and chemical industry, and particularly discloses a method and a device for efficiently regenerating amine liquid of a coupling heat pump, wherein the method comprises the following steps of exchanging heat of a stream of rich amine liquid through a liquid heat exchanger, then introducing the heat exchange heat into a regeneration tower for regeneration, and carrying out desorption and separation on carbon dioxide absorbed in the stream of rich amine liquid to obtain carbon dioxide and lean amine liquid; the other stream of rich amine liquid is subjected to heat exchange through a gas-liquid heat exchanger, then is introduced into a regeneration tower for regeneration, and carbon dioxide absorbed in the stream of rich amine liquid is subjected to desorption and separation to obtain carbon dioxide and lean amine liquid; the lean amine liquid desorbed and separated by the regeneration tower is at least led into a liquid heat exchanger to participate in heat exchange of the rich amine liquid; and the carbon dioxide desorbed and separated by the regeneration tower is at least introduced into a gas-liquid heat exchanger to exchange heat with the rich amine liquid. Thoroughly solves the problem of high energy consumption of the decarbonization process in the existing amine liquid regeneration method and the device thereof.
Description
Technical Field
The invention relates to the technical field of energy and chemical industry, in particular to a method and a device for efficiently regenerating amine liquid of a coupling heat pump.
Background
With the gradual increase of the global natural gas demandThe LNG (liquefied natural gas ) industry is coming to a good prospect. Due to the CO contained in the natural gas 2 、H 2 S, organic sulfur and other acid gas impurities, and under the low-temperature environment, the impurities have corrosion effects on equipment and freeze and block pipelines, equipment and valves due to low temperature. Must undergo a deep purification treatment, especially CO, before entering the LNG liquefaction 2 Whether the pretreatment of gas and impurities can reach specific deep purification indexes directly affects a liquefaction system or not, so that the process of deep decarbonization and purification of natural gas is particularly important.
At present, the deep decarbonization process of natural gas mainly adopts a solvent (physical or chemical) absorption method, wherein lean solution and gas are in countercurrent absorption of CO in an absorption tower 2 Becomes rich liquid, and the rich liquid is used for removing the absorbed CO in the desorption tower at high temperature 2 So as to realize regeneration, the desorption regeneration process of the rich liquid is an extremely important ring in an amine liquid circulation process method in a solvent absorption method; the conventional natural gas deep decarbonization process has the advantages of high energy consumption, high temperature of a regeneration tower, overlarge load of a reboiler, simple process flow heat exchange, small integration level of a heat exchange network and high heat loss, and meanwhile, the conventional desorption tower has the problems of weak gas-liquid mass transfer, easy blockage of filling and low efficiency.
Therefore, a novel process and a device thereof are studied to overcome the above problems so as to reduce the energy consumption of the rich liquid regeneration device.
Disclosure of Invention
The invention aims to provide a method and a device for efficiently regenerating an amine liquid of a coupled heat pump, which are used for solving the problem of high energy consumption of a decarbonization process in the existing method and device for regenerating the amine liquid.
In order to solve the technical problems, the invention provides a method for efficiently regenerating an amine liquid of a coupling heat pump, which comprises the steps of exchanging heat of a stream of rich amine liquid through a liquid heat exchanger, then introducing the stream of rich amine liquid into a regeneration tower for regeneration, and desorbing and separating carbon dioxide absorbed in the stream of rich amine liquid to obtain carbon dioxide and lean amine liquid; the other stream of rich amine liquid is subjected to heat exchange through a gas-liquid heat exchanger, then is introduced into a regeneration tower for regeneration, and carbon dioxide absorbed in the stream of rich amine liquid is subjected to desorption and separation to obtain carbon dioxide and lean amine liquid; the lean amine liquid desorbed and separated by the regeneration tower is at least led into a liquid heat exchanger to participate in heat exchange of the rich amine liquid; and the carbon dioxide desorbed and separated by the regeneration tower is at least introduced into a gas-liquid heat exchanger to exchange heat with the rich amine liquid.
In one embodiment, the desorption and separation are carried out on the rich amine liquid after heat exchange in the regeneration tower, and the method comprises the following steps that the rich amine liquid after heat exchange is subjected to cyclone desorption through the spiral inner cylinder so as to separate amine liquid and carbon dioxide; the amine liquid after cyclone desorption is heated for the second time through a reheating inner cylinder; and (3) carrying out reheat desorption on the amine liquid subjected to secondary heating through a regeneration inner barrel so as to separate lean amine liquid and carbon dioxide.
In one embodiment, carbon dioxide desorbed and separated by the regeneration tower is introduced into a compressor for compression, and the compressed carbon dioxide is introduced into a gas-liquid heat exchanger for heat exchange.
In one embodiment, the desorption separation is performed in the regenerator at a temperature of 100 to 120 ℃.
In one embodiment, the temperature of the heat exchange medium in the lean rich amine liquid heat exchanger is 90-120 ℃.
In one embodiment, the temperature of the heat exchange medium in the gas-liquid heat exchanger is 90-120 ℃.
In one embodiment, carbon dioxide subjected to heat exchange in the gas-liquid heat exchanger is introduced into the sour gas cooler and then discharged.
In order to solve the technical problems, the invention provides a device for efficiently regenerating the amine liquid of a coupling heat pump, and a method for efficiently regenerating the amine liquid of the coupling heat pump is applied; the device comprises a liquid heat exchanger, a regeneration tower and a gas-liquid heat exchanger; the liquid heat exchanger is communicated with the regeneration tower, and the regeneration tower is also communicated with the gas-liquid heat exchanger; the regeneration tower is used for carrying out cyclone desorption and reheat desorption on the rich amine liquid so as to separate lean liquid and carbon dioxide.
In one embodiment, the top of the regeneration tower is provided with a plurality of liquid inlets and air outlets, the bottom of the regeneration tower is provided with a liquid outlet, the side wall of the regeneration tower is provided with a plurality of first mounting holes, and the plurality of first mounting holes are provided with steam pipelines; the inside of the regeneration tower is sequentially connected with a spiral inner cylinder, a reheating inner cylinder and a regeneration inner cylinder along the liquid outflow direction; the diameter of the spiral cylinder is linearly narrowed along the outflow direction of the liquid, the upper surface of the inner wall of the spiral cylinder is abutted with ribs which are spirally arranged along the inner wall of the spiral cylinder, and the spiral cylinder is used for carrying out cyclone desorption on the rich amine liquid so as to separate the amine liquid and the carbon dioxide; a plurality of inclined flow layers are arranged in the reheating inner cylinder, the plurality of inclined flow layers are arranged in a staggered manner, and a first gap is reserved between adjacent inclined flow layers; each diagonal flow layer comprises a plurality of diagonal flow plates, the diagonal flow plates are uniformly arranged, and a second gap is reserved between every two adjacent diagonal flow plates; the side wall of the reheating inner barrel is provided with a second mounting hole, and a steam pipeline is arranged in the second mounting hole; the diameter of the regeneration inner cylinder is linearly widened along the liquid outflow direction, and the regeneration inner cylinder is used for carrying out reheat desorption on the reheated amine liquid so as to separate lean liquid and carbon dioxide.
In one embodiment, a plurality of baffle plates are arranged in the regeneration inner cylinder, the baffle plates are uniformly arranged, and a third gap is reserved between every two adjacent baffle plates.
In one embodiment, the device for efficiently regenerating the amine liquid of the coupled heat pump further comprises a compressor, wherein an air inlet of the compressor is communicated with the regeneration tower, and an air outlet of the compressor is connected with the ventilation liquid heat exchanger.
In one embodiment, the device for efficiently regenerating the amine liquid of the coupled heat pump further comprises an acid gas cooler, wherein the acid gas cooler is communicated with the air outlet of the gas-liquid heat exchanger.
The beneficial effects of the invention are as follows:
because one stream of rich amine liquid exchanges heat with the liquid heat exchanger and then is introduced into the regeneration tower for regeneration, carbon dioxide and lean amine liquid are obtained by desorption and separation of carbon dioxide absorbed in the stream of rich amine liquid, and the lean amine liquid desorbed and separated by the regeneration tower is at least introduced into the liquid heat exchanger to participate in the heat exchange of the rich amine liquid, when the rich amine liquid is applied, the stream of rich amine liquid exchanges heat with a lean amine liquid heat source desorbed and separated in the regeneration tower before entering the regeneration tower, so that the aim of preheating the rich amine liquid is achieved, namely, a certain temperature is reserved for the stream of rich amine liquid before being introduced into the regeneration tower, and the heating energy consumption of the rich amine liquid in the regeneration tower is saved.
Because the other stream of rich amine liquid exchanges heat through the gas-liquid heat exchanger and then is introduced into the regeneration tower for regeneration, the carbon dioxide absorbed in the stream of rich amine liquid is desorbed and separated to obtain carbon dioxide and lean amine liquid, and the carbon dioxide desorbed and separated by the regeneration tower is at least introduced into the gas-liquid heat exchanger for heat exchange with the rich amine liquid, when the heat exchange device is applied, the stream of rich amine liquid exchanges heat with a carbon dioxide heat source desorbed and separated in the regeneration tower before entering the regeneration tower, so that the aim of preheating the rich amine liquid is fulfilled, a certain temperature is reserved for the stream of rich amine liquid before being introduced into the regeneration tower, the consumption of a tower top condenser, cooling water and heating steam of a reboiler of the regeneration tower is saved, and the heat loss of the regeneration tower is reduced.
Because the regeneration tower is used for carrying out cyclone desorption and reheat desorption on the rich amine liquid, when the regeneration tower is used, the rich amine liquid is subjected to cyclone desorption in the regeneration tower, and the amine liquid subjected to cyclone desorption can be reheated to form secondary regeneration, so that the regeneration strength is increased, and the regeneration effect of the regeneration tower is improved.
In summary, heat exchange is performed before the rich amine liquid enters the regeneration tower, so that the temperature before the rich amine liquid enters the regeneration tower is increased, the energy consumption for heating the rich amine liquid to the required temperature in the regeneration tower is reduced, and the regeneration tower is internally provided with cyclone desorption and reheat desorption functions, so that the regeneration strength is improved, the regeneration effect of the regeneration tower is effectively improved, and the problem of high energy consumption of the decarburization process in the conventional amine liquid regeneration method and device is thoroughly solved.
Drawings
In order to more clearly illustrate the technical solutions of the present invention, the drawings that are needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic view of the overall structure provided by the preferred embodiment of the present invention;
FIG. 2 is a schematic view of a regenerator structure provided in a preferred embodiment of the present invention;
fig. 3 is a schematic view showing the internal structure of a regenerator provided in a preferred embodiment of the present invention.
The reference numerals are as follows:
1. a liquid heat exchanger;
2. a regeneration tower; 20. a liquid inlet; 21. an air outlet; 22. a liquid outlet; 23. a steam line; 24. a spiral inner cylinder; 240. a rib; 25. reheat inner tube; 250. a diagonal flow layer; 2500. a diagonal flow plate; 2501. a second gap; 251. a first gap; 26. a regeneration inner cylinder; 260. a baffle plate; 261. a third gap;
3. a gas-liquid heat exchanger;
4. a compressor;
5. an acid gas cooler.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention.
In the prior art, the energy consumption of the regeneration process is large, and the problems are mainly represented in two major problems, namely, the problem of low heat exchange efficiency of the heat exchange of the rich amine liquid exists, particularly, the heat exchange of the existing low-temperature rich amine liquid is only carried out with the regenerated high-temperature lean amine liquid, and all low Wen Fuan liquid exchanges heat with the high-temperature lean amine liquid, so that the heat exchange efficiency is low; secondly, the amine liquid needs to be additionally reheated when the amine liquid is regenerated, specifically, the existing regeneration process needs to use a reboiler to reheat the amine liquid after primary regeneration outside a regeneration tower, and energy is required to be additionally consumed.
In order to solve the problems, the invention improves the process through the technical characteristics of two directions; firstly, the rich amine liquid is divided into two parts before entering the regeneration tower, one part exchanges heat with the lean amine liquid separated by the regeneration tower, and the other part exchanges heat with the carbon dioxide separated by the regeneration tower; and a device with a reheating function is arranged in the regeneration tower.
Specifically, as shown in fig. 1, the invention provides a method for efficiently regenerating an amine liquid of a coupled heat pump, which comprises the following steps:
s1, separating rich amine liquid absorbed with carbon dioxide into two streams;
s2, exchanging heat between a stream of rich amine liquid and the liquid heat exchanger 1, introducing the rich amine liquid after heat exchange into the regeneration tower 2, and desorbing and separating carbon dioxide absorbed by the stream of rich amine liquid to obtain carbon dioxide and lean amine liquid; the other strand exchanges heat with the gas-liquid heat exchanger 3, the rich amine liquid after heat exchange is introduced into the regeneration tower 2, and the carbon dioxide absorbed by the rich amine liquid is desorbed and separated to obtain carbon dioxide and lean amine liquid;
wherein, the lean amine liquid after the analysis and separation of the regeneration tower 2 is at least introduced into the liquid heat exchanger 1 to participate in the heat exchange of the rich amine liquid, and the carbon dioxide after the analysis and separation of the regeneration tower 2 is at least introduced into the gas-liquid heat exchanger 3 to participate in the heat conversion of the rich amine liquid.
And S3, discharging the separated carbon dioxide after heat exchange of the gas-liquid heat exchanger 3, and discharging the separated lean amine liquid after heat exchange of the liquid heat exchanger 1.
By the method, lean amine liquid after the analysis and separation of the regeneration tower 2 is introduced into the liquid heat exchanger 1 for heat exchange, carbon dioxide after the analysis and separation of the regeneration tower 2 is introduced into the gas-liquid heat exchanger 3 for heat exchange, besides the heat of the desorbed lean amine liquid is used for heat exchange, the heat of the desorbed carbon dioxide is also used for heat exchange, i.e. the latent heat of the tower body of the regeneration tower 2 is used for the system, so that the consumption of a condenser at the top of the regeneration tower 2, cooling water and heating steam of a reboiler is saved, the energy consumption of the process is obviously reduced, and the problem that the heat exchange is insufficient due to the large heat exchange amount of the lean amine liquid after the analysis and separation of the rich amine liquid is only introduced into the liquid heat exchanger 1 and the regeneration tower in the prior art is avoided.
In the related step S1, as shown in fig. 1 to 3, the rich amine liquid after absorbing carbon dioxide is separated into two strands by the tee pipe, so that the two strands of rich amine liquid can exchange heat with different heat exchange media, the single strand heat exchange efficiency is improved, and the problem that in the prior art, all rich amine liquid exchanges heat with the same heat exchange medium, and the heat exchange efficiency is low is avoided.
It should be noted that the rich amine liquid after absorbing carbon dioxide can be divided into two streams, and can be divided into multiple streams through a multi-way pipe, so long as the fact that the multiple streams of rich amine liquid can exchange heat with different heat exchange media is satisfied, namely the concept of the invention is met, and the rich amine liquid can be selected by a person skilled in the art according to actual demands.
As shown in fig. 1 to 3, in step S2, the regeneration tower 2 desorbs the heat-exchanged amine-rich liquid, and further includes the steps of:
s2-1, performing cyclone desorption on the rich amine liquid subjected to heat exchange through a spiral inner cylinder 24 to separate amine liquid and carbon dioxide;
s2-2, performing secondary heating on the amine liquid subjected to cyclone desorption through a reheating inner barrel 25;
in step S2-3, the amine liquid after secondary heating is subject to reheat desorption through the regeneration inner cylinder 26 to separate lean amine liquid and carbon dioxide.
Through the method, after the rich amine liquid enters the regeneration tower 2, cyclone analysis is firstly carried out, carbon dioxide in the rich amine liquid and the amine liquid are subjected to gas-liquid separation under the action of centrifugal force, the rich amine liquid is regenerated for the first time in the process, then the rich amine liquid is heated for the second time in the regeneration tower 2, the regenerated amine liquid reaches the regeneration temperature again, and the carbon dioxide and the amine liquid are subjected to gas-liquid separation again, so that the secondary regeneration effect is achieved, the condition that a reboiler is additionally arranged outside the regeneration tower 2 to reheat the regenerated amine liquid for the first time in the prior art is avoided, the occupied area is reduced, the regeneration efficiency is improved, and the overall economic benefit is increased.
Further, in order to meet the desorption separation requirement in the regeneration tower 2, as shown in fig. 1 to 3, the desorption separation is performed in the regeneration tower 2 at a temperature of 100 to 120 ℃.
The temperature of the heat-exchanged rich amine liquid entering the regeneration tower is 100 ℃, cyclone analysis separation is carried out at the temperature, then the regenerated rich amine liquid is introduced into the spiral inner cylinder 24 for secondary heating, the rich amine liquid after the secondary heating is heated to 110 ℃ under the heating of the steam pipeline 23, and then secondary regeneration is carried out.
By such an arrangement, the rich amine liquid entering the regeneration tower 2 can be subjected to amine liquid regeneration at that temperature to desorb and separate carbon dioxide and lean amine liquid.
In step S3, as shown in fig. 1 to 3, carbon dioxide desorbed and separated by the regeneration tower 2 is introduced into the compressor 4 to be compressed, and the compressed carbon dioxide is introduced into the gas-liquid heat exchanger 3 to participate in heat exchange.
By the method, the separated carbon dioxide is compressed and acted by the compressor 4 to improve the heat energy quality, namely, the compressor 4 is utilized to provide certain mechanical work for the process method, the mechanical work is converted into heat energy, the heat energy quality of the gas phase at the top of the regeneration tower 2 can be effectively improved, and the heat energy quality is used as a heat source medium for heat exchange of the regeneration tower 2.
Further, in order to improve the heat exchange efficiency of the rich amine liquid in the liquid heat exchanger 1, as shown in fig. 1 to 3, the lean amine liquid after separation is introduced into the liquid heat exchanger 1, and the temperature as a heat exchange medium is 90 to 120 ℃.
Further, in order to improve the heat exchange efficiency of the rich amine liquid in the gas-liquid heat exchanger 3, as shown in fig. 1 to 3, the separated carbon dioxide is introduced into the gas-liquid heat exchanger 3, and the temperature as a heat exchange medium is 90-120 DEG C
By such an arrangement, the rich amine liquid has a higher heat exchange efficiency in the liquid heat exchanger 1.
Further, in order to reduce the influence of the ammonia-containing carbon dioxide on the environment, as shown in fig. 1 to 3, carbon dioxide subjected to heat exchange in the gas-liquid heat exchanger 3 is introduced into the sour gas cooler 5 and then discharged.
With such an arrangement, the carbon dioxide is subjected to an ammonia removal operation by the acid gas cooler 5 before being discharged, and the influence of the discharged carbon dioxide on the environment is reduced.
From the foregoing, it can be seen that the present invention provides a method for efficiently regenerating an amine liquid coupled to a heat pump, and an apparatus for efficiently regenerating an amine liquid coupled to a heat pump will be described in detail.
Specifically, as shown in fig. 1 to 3, a device for efficiently regenerating amine liquid of a coupled heat pump comprises a liquid heat exchanger 1, a regeneration tower 2, a gas-liquid heat exchanger 3, a compressor 4 and an acid gas cooler 5; the liquid heat exchanger 1 is communicated with the regeneration tower 2, the regeneration tower 2 is also communicated with the compressor 4 and the gas-liquid heat exchanger 3, the compressor 4 is communicated with the gas-liquid heat exchanger 3, and the gas-liquid heat exchanger 3 is also communicated with the acid gas cooler 5.
The liquid inlet 20 of the liquid heat exchanger 1 is respectively connected with a rich amine liquid inlet channel and a liquid outlet 22 of the regeneration tower 2, the liquid outlet 22 of the liquid heat exchanger 1 is respectively connected with a lean amine liquid outlet channel and the liquid inlet 20 of the regeneration tower 2, the air outlet 21 of the regeneration tower 2 is connected with the air inlet of the compressor 4, the air outlet 21 of the compressor 4 is connected with the air inlet of the ventilation liquid heat exchanger 3, the liquid inlet 20 of the gas-liquid heat exchanger 3 is connected with the rich amine liquid inlet channel, and the air outlet 21 of the gas-liquid heat exchanger 3 is connected with the acid gas cooler 5 and then discharged.
When the method is applied, the rich amine liquid is divided into two streams, one stream is introduced into the liquid heat exchanger 1 to exchange heat, the other stream is introduced into the gas-liquid heat exchanger 3 to exchange heat, the rich amine liquid after heat exchange is introduced into the regeneration tower 2, the rich amine liquid is subjected to cyclone desorption and reheat desorption in the regeneration tower 2, carbon dioxide absorbed by the rich amine liquid is separated, carbon dioxide and lean amine liquid without carbon dioxide are formed, the separated lean amine liquid is introduced into the liquid heat exchanger 1 to exchange heat, carbon dioxide of the next cycle is then absorbed, the separated carbon dioxide is firstly introduced into the compressor 4 to perform compression work to improve heat energy quality, and then the carbon dioxide is introduced into the gas-liquid heat exchanger 3 to exchange heat, and is discharged through the acid gas cooler 5.
Regarding the above-mentioned regeneration tower 2, as shown in fig. 1 to 3, the top of the regeneration tower 2 is provided with two liquid inlets 20 and two air outlets 21, the bottom of the regeneration tower 2 is provided with a liquid outlet 22, the side wall of the regeneration tower 2 is provided with two first mounting holes, and the two first mounting holes are provided with a steam pipeline 23; the inside of the regeneration tower 2 is sequentially connected with a spiral inner cylinder 24, a reheating inner cylinder 25 and a regeneration inner cylinder 26 along the liquid outflow direction; the spiral cylinder is used for carrying out cyclone desorption on the amine-rich liquid so as to separate out amine liquid and carbon dioxide; a steam pipeline 23 is arranged in the reheating inner cylinder 25, and the reheating inner cylinder 25 is used for reheating the rich amine liquid to reach the temperature required by regeneration; the regeneration drum 26 is used for reheat desorption of the reheated amine solution to separate lean amine solution and carbon dioxide.
Wherein, the two liquid inlets 20 and the inner wall of the regeneration tower 2 form tangential arrangement, so that the rich amine liquid entering from the liquid inlets 20 can form rotational flow along the tangential direction; the separated carbon dioxide is led out of the regeneration tower 2 from an air outlet 21 at the top of the tower body; the top of the spiral inner tube 24 is in contact with the inner wall of the regeneration tower 2, and the bottom of the regeneration inner tube 26 is in contact with the inner wall of the regeneration tower 2.
When the method is applied, after the rich amine liquid enters the regeneration tower 2, a rotational flow is formed in the spiral inner cylinder 24, the gas-liquid separation effect is achieved under the centrifugal effect, the rich amine liquid after the gas-liquid separation is reheated through the steam pipeline 23 of the reheating inner cylinder 25 to reach the regeneration temperature, the rich amine liquid after the temperature is fully regenerated in the regeneration inner cylinder 26 to separate carbon dioxide and lean amine liquid, the separated carbon dioxide is discharged through the gas outlet 21 at the tower top, and the separated lean amine liquid is discharged through the liquid outlet 22 at the tower bottom.
For the spiral inner cylinder 24, as shown in fig. 3, the cylinder diameter of the spiral cylinder is linearly narrowed along the outflow direction of the liquid to form an inverted circular truncated cone-shaped structure, and the rib 240 provided on the spiral inner cylinder 24 makes the rich amine liquid swirl on the rib 240 to complete swirl desorption.
When the method is applied, the spiral desorption mode can lead the rich amine liquid to fully separate the absorbed carbon dioxide through spiral desorption.
For the reheating inner cylinder 25, as shown in fig. 3, three diagonal layers 250 are arranged in the reheating inner cylinder 25, the three diagonal layers 250 are staggered, and a first gap 251 is reserved between adjacent diagonal layers 250; each diagonal flow layer 250 comprises six diagonal flow plates 2500, the six diagonal flow plates 2500 are uniformly arranged, and a second gap 2501 is reserved between adjacent diagonal flow plates 2500.
The inner wall of the reheating inner barrel 25 is further provided with two second mounting holes, the two second mounting holes are internally provided with steam pipelines 23, the steam pipelines 23 penetrate through three inclined flow layers 250, amine liquid flowing through different inclined flow layers 250 can exchange heat with the steam pipelines 23, and each time the amine liquid flows through the inclined flow layers 250, the amine liquid can exchange heat with the steam pipelines 23, so that the amine liquid can be heated to a required temperature.
It should be noted that the steam pipe 23 is preferably a U-shaped structure, and other structures capable of passing through the three diagonal layers 250 can be used, and those skilled in the art can select the structure according to their actual needs.
When the method is applied, the amine liquid regenerated at the upper section enters into the first contact with the steam pipeline 23 through the first inclined flow layer 250, flows into the second inclined flow layer 250 to contact with the steam pipeline 23 for the second time, then enters into the regeneration inner cylinder 26 through the third inclined flow layer 250 to contact with the steam pipeline 23 for the third time so as to reach the regeneration temperature of the amine liquid again, and the problem that a reboiler is additionally arranged outside the regeneration tower 2 to reheat the amine liquid regenerated for the first time in the prior art is avoided.
As shown in fig. 3, the regeneration inner tube 26 has a circular truncated cone-shaped structure in which the tube diameter of the regeneration inner tube 26 is linearly widened in the liquid outflow direction, a plurality of baffles 260 are provided in the regeneration inner tube 26, the plurality of baffles 260 are uniformly arranged, and a third gap 261 is provided between adjacent baffles 260.
Wherein, each baffle 260 is vertically arranged, and the vertical section of each baffle 260 is a Z-shaped head-tail connection structure.
When the device is applied, the reheated amine liquid enters the baffle plate 260, and the amine liquid is divided into a plurality of streams under the action of the baffle plate 260, so that the effect of full regeneration is achieved.
The specific procedure when the apparatus applies the method will be described below.
The rich amine liquid after fully absorbing carbon dioxide is divided into two streams; the first stream of rich amine liquid exchanges heat through a liquid heat exchanger 1, and the second stream of rich amine liquid exchanges heat through a gas-liquid heat exchanger 3; the rich amine liquid after heat exchange enters a regeneration tower 2 from the tower top, and carbon dioxide absorbed in the rich amine liquid is desorbed and separated; the rich amine liquid tangentially enters the regeneration tower 2 from two liquid inlets 20 at the top of the tower, firstly, the rich amine liquid flows into a spiral inner cylinder 24, a rotational flow is formed under the action of a spiral rib 240, carbon dioxide absorbed by the rich amine liquid is desorbed through centrifugal force, the desorbed amine liquid enters a reheating inner cylinder 25 through an inclined flow plate 2500, a steam pipeline 23 is arranged in the reheating inner cylinder 25 to reheat the amine liquid, the reheated amine liquid passes through a baffle plate 260, and under the action of the baffle plate 260, the amine liquid is divided into a plurality of streams to achieve a full regeneration effect, the fully regenerated amine liquid flows out from the bottom of the regeneration tower 2, then the lean amine liquid enters a liquid heat exchanger 1 to exchange heat with a first rich amine liquid, and then is discharged; the carbon dioxide flows out from the top of the regeneration tower 2, enters the gas-liquid heat exchanger 3 after passing through the compressor 4 to exchange heat with the second stream of amine-rich liquid, and is cooled and discharged through the acid gas cooler 5.
While the foregoing is directed to the preferred embodiments of the present invention, it will be appreciated by those skilled in the art that changes and modifications may be made without departing from the principles of the invention, such changes and modifications are also intended to be within the scope of the invention.
Claims (3)
1. The device for efficiently regenerating the amine liquid of the coupling heat pump is characterized by comprising a liquid heat exchanger, a regeneration tower and a gas-liquid heat exchanger;
the liquid heat exchanger is communicated with the regeneration tower, and the regeneration tower is also communicated with the gas-liquid heat exchanger;
the regeneration tower is used for carrying out cyclone desorption and reheat desorption on the rich amine liquid so as to separate lean liquid and carbon dioxide;
the top of the regeneration tower is provided with an air outlet and two liquid inlets, and the bottom of the regeneration tower is provided with a liquid outlet;
the inside of the regeneration tower is sequentially connected with a spiral inner cylinder, a reheating inner cylinder and a regeneration inner cylinder along the liquid outflow direction;
the diameter of the spiral inner cylinder is linearly narrowed along the flowing-out direction of the liquid, the upper surface of the inner wall of the spiral inner cylinder is abutted with ribs, the ribs are spirally arranged along the inner wall of the spiral inner cylinder, and the spiral inner cylinder is used for carrying out cyclone desorption on the rich amine liquid so as to separate the amine liquid and the carbon dioxide;
a plurality of diagonal layers are arranged in the reheating inner cylinder, the diagonal layers are arranged in a staggered mode, and a first gap is reserved between every two adjacent diagonal layers; each diagonal flow layer comprises a plurality of diagonal flow plates, the diagonal flow plates are uniformly arranged, and a second gap is reserved between every two adjacent diagonal flow plates; a second mounting hole is formed in the side wall of the reheating inner barrel, and a steam pipeline is mounted in the second mounting hole;
the diameter of the regeneration inner cylinder is linearly widened along the liquid outflow direction, and the regeneration inner cylinder is used for carrying out reheat desorption on the reheated amine liquid so as to separate lean liquid and carbon dioxide;
the method for the device for efficiently regenerating the amine liquid by adopting the coupling heat pump comprises the following steps of:
separating the rich amine liquid after absorbing the carbon dioxide into two streams;
carrying out heat exchange on a stream of rich amine liquid through a liquid heat exchanger, then introducing the rich amine liquid into a regeneration tower for regeneration, and carrying out desorption separation on carbon dioxide absorbed in the stream of rich amine liquid to obtain carbon dioxide and lean amine liquid;
the other stream of rich amine liquid is subjected to heat exchange through a gas-liquid heat exchanger, then is introduced into a regeneration tower for regeneration, and carbon dioxide absorbed in the stream of rich amine liquid is subjected to desorption and separation to obtain carbon dioxide and lean amine liquid;
wherein,
the lean amine liquid desorbed and separated by the regeneration tower is at least led into a liquid heat exchanger to participate in the heat exchange of the rich amine liquid;
and the carbon dioxide desorbed and separated by the regeneration tower is at least introduced into a gas-liquid heat exchanger to exchange heat with the rich amine liquid.
2. The device for efficiently regenerating amine liquid of a coupled heat pump according to claim 1, wherein,
the regeneration inner barrel is internally provided with a plurality of baffle plates, a plurality of baffle plates are uniformly arranged, and a third gap is reserved between every two adjacent baffle plates.
3. The device for efficiently regenerating amine liquid of a coupled heat pump according to claim 1, wherein,
the device for efficiently regenerating the amine liquid of the coupling heat pump also comprises a compressor, wherein an air inlet of the compressor is communicated with the regeneration tower, and an air outlet of the compressor is communicated with the gas-liquid heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310339391.9A CN116445196B (en) | 2023-04-03 | 2023-04-03 | Method and device for efficiently regenerating amine liquid of coupling heat pump |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310339391.9A CN116445196B (en) | 2023-04-03 | 2023-04-03 | Method and device for efficiently regenerating amine liquid of coupling heat pump |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN116445196A CN116445196A (en) | 2023-07-18 |
| CN116445196B true CN116445196B (en) | 2024-03-19 |
Family
ID=87119488
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310339391.9A Active CN116445196B (en) | 2023-04-03 | 2023-04-03 | Method and device for efficiently regenerating amine liquid of coupling heat pump |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116445196B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013161574A1 (en) * | 2012-04-24 | 2013-10-31 | 三菱重工業株式会社 | Co2 recovery device, and co2 recovery method |
| CN103463955A (en) * | 2013-09-16 | 2013-12-25 | 湖南大学 | Technology for separating and recovering carbon dioxide from industrial tail gas |
| CN108048147A (en) * | 2018-01-26 | 2018-05-18 | 中海石油气电集团有限责任公司 | A kind of amine liquid regenerative system and technique applied to Floating Liquefied Natural Gas facility |
| CN109954289A (en) * | 2017-12-22 | 2019-07-02 | 上海华畅环保设备发展有限公司 | Desulfurization rich amine solution eddy flow strengthens de- hydrocarbon method and apparatus |
| CN110038646A (en) * | 2019-05-30 | 2019-07-23 | 国电环境保护研究院有限公司 | A kind of carbon base catalyst regenerating unit and technique |
-
2023
- 2023-04-03 CN CN202310339391.9A patent/CN116445196B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013161574A1 (en) * | 2012-04-24 | 2013-10-31 | 三菱重工業株式会社 | Co2 recovery device, and co2 recovery method |
| CN103463955A (en) * | 2013-09-16 | 2013-12-25 | 湖南大学 | Technology for separating and recovering carbon dioxide from industrial tail gas |
| CN109954289A (en) * | 2017-12-22 | 2019-07-02 | 上海华畅环保设备发展有限公司 | Desulfurization rich amine solution eddy flow strengthens de- hydrocarbon method and apparatus |
| CN108048147A (en) * | 2018-01-26 | 2018-05-18 | 中海石油气电集团有限责任公司 | A kind of amine liquid regenerative system and technique applied to Floating Liquefied Natural Gas facility |
| CN110038646A (en) * | 2019-05-30 | 2019-07-23 | 国电环境保护研究院有限公司 | A kind of carbon base catalyst regenerating unit and technique |
Non-Patent Citations (1)
| Title |
|---|
| 潘灼南等.《氮肥工业》.中国工业出版社,1964,第255-256页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN116445196A (en) | 2023-07-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2011122559A1 (en) | Carbon dioxide gas recovery device | |
| WO2011122525A1 (en) | Carbon dioxide gas recovery device | |
| CN110115910A (en) | A kind of energy-saving carbon dioxide capture system and method | |
| CN107261754B (en) | VOCs waste gas recovery treatment method and device | |
| CA2897489C (en) | Dehydration equipment, gas compression system, and dehydration method | |
| CN108744893B (en) | CO based on heat pipe enhanced heat recovery 2 Chemical absorption system and method | |
| WO2021093262A1 (en) | Vocs recovery system and method integrating absorption, desorption and recovery | |
| CN205933758U (en) | Condensing vapor recovery system equipment | |
| CN108211671B (en) | Energy-saving carbon dioxide regeneration and compression system and method | |
| CN102502901B (en) | Condensed fluid stripping method matched with CO transforming device | |
| CN111849578A (en) | Containing CO at a high concentration2Device and process for gas decarburization and amine liquid regeneration | |
| CN107297132A (en) | A kind of ionic liquid absorption cycle flue gas desulfurization device and its method | |
| CN116445196B (en) | Method and device for efficiently regenerating amine liquid of coupling heat pump | |
| CN105749728A (en) | Carbon dioxide trapping method and device thereof | |
| CN116078116B (en) | Container-type modularized ship tail gas carbon capture system | |
| CN111036040A (en) | Condensation-adsorption integrated VOCs recycling system and recycling process | |
| CN217410284U (en) | Novel chemical absorption method flue gas CO2 entrapment system | |
| CN205556590U (en) | Double tower that is suitable for transportation of sled piece absorbs palingenetic natural gas deacidification equipment of double tower | |
| CN209024471U (en) | A kind of multi-joint-production apparatus being pyrolyzed coal gas hydrogen rich gas, LNG, mixed hydrocarbon | |
| CN212560132U (en) | Containing CO at a high concentration2Device for gas decarbonization and amine liquid regeneration | |
| CN112246075A (en) | Ammonia washing tower, and anti-corrosion conversion gas ammonia washing device and process using same | |
| CN220939890U (en) | Carbon dioxide trapping and processing integrated device for flue gas discharged by natural gas boiler | |
| CN205386395U (en) | Use new material and optimize absorption tower | |
| CN217340799U (en) | Coal-fired power plant flue gas CO based on energy conservation and emission reduction 2 Trapping system | |
| CN215654540U (en) | Waste gas collecting device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |