CN221619022U - System for high-efficient separation carbon monoxide, carbon dioxide and hydrogen sulfide - Google Patents
System for high-efficient separation carbon monoxide, carbon dioxide and hydrogen sulfide Download PDFInfo
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- CN221619022U CN221619022U CN202323421697.3U CN202323421697U CN221619022U CN 221619022 U CN221619022 U CN 221619022U CN 202323421697 U CN202323421697 U CN 202323421697U CN 221619022 U CN221619022 U CN 221619022U
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 92
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 229910000037 hydrogen sulfide Inorganic materials 0.000 title claims abstract description 50
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 46
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 46
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 229910002091 carbon monoxide Inorganic materials 0.000 title claims abstract description 37
- 238000000926 separation method Methods 0.000 title claims abstract description 15
- 239000007788 liquid Substances 0.000 claims abstract description 70
- 238000010521 absorption reaction Methods 0.000 claims abstract description 66
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 30
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 28
- 239000011593 sulfur Substances 0.000 claims abstract description 28
- 239000006260 foam Substances 0.000 claims abstract description 25
- 230000008929 regeneration Effects 0.000 claims abstract description 25
- 238000011069 regeneration method Methods 0.000 claims abstract description 25
- 238000001914 filtration Methods 0.000 claims abstract description 16
- 238000011033 desalting Methods 0.000 claims abstract description 11
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 11
- 239000011347 resin Substances 0.000 claims description 7
- 229920005989 resin Polymers 0.000 claims description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 4
- 239000003456 ion exchange resin Substances 0.000 claims description 4
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 4
- 239000004744 fabric Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 41
- 238000000034 method Methods 0.000 abstract description 10
- 239000007791 liquid phase Substances 0.000 description 13
- 238000006460 hydrolysis reaction Methods 0.000 description 9
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 7
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 7
- 230000007062 hydrolysis Effects 0.000 description 7
- 239000012071 phase Substances 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 5
- 239000012535 impurity Substances 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000012856 packing Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 239000005997 Calcium carbide Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 description 1
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- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide, which comprises an absorption tower I, a heat exchanger I, a gas-liquid separator I, a solution filtering device, a heat exchanger II, a heat exchanger III, a solution desalting device, a lean liquid pump, a solution pump, a semi-lean liquid pump, a normal Jie Qidi tower, a reboiler, a heat exchanger IV, a gas-liquid separator II, an absorption tower II, a desulfurizing tower, a rich liquid pump, a regeneration tank, a sulfur foam tank and a sulfur foam pump. The system has the advantages of simple process flow, high separation efficiency, capability of selectively separating carbon monoxide, carbon dioxide and hydrogen sulfide gases respectively, and stable long-period operation.
Description
Technical Field
The utility model belongs to the field of gas separation, and is particularly suitable for separating gas containing carbon monoxide, carbon dioxide and hydrogen sulfide.
Background
In the process of producing glycol from calcium carbide furnace gas, coke oven gas and coal gasification synthetic gas, a conversion process is often adopted to ensure that the hydrogen concentration of raw material gas is higher than that of carbon monoxide, a sulfur-resistant catalyst is used in the conversion process, and a certain amount of H 2 S is needed to maintain the activity of the catalyst so as to prevent the catalyst from being vulcanized reversely. Therefore, in order to separate and purify carbon monoxide and hydrogen in the raw material gas and remove impurity gases such as carbon dioxide, hydrogen sulfide and the like, a system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is required.
Patent CN110835556a describes a wet desulfurization system and method for blast furnace gas, the specific device includes a hydrolysis reactor for hydrolysis reaction of gas and a solution absorption tank for absorbing sulfur-containing gas, the hydrolysis reactor is filled with hydrolysis catalyst, the gas inlet of the hydrolysis reactor is equipped with a gas inlet pipe, the gas outlet of the hydrolysis reactor is equipped with a gas outlet pipe, the gas inlet pipe and the gas outlet pipe are respectively equipped with a first gas sampling port and a second gas sampling port, the solution absorption tank is communicated with the hydrolysis reactor through the gas outlet pipe, the gas outlet of the solution absorption tank is equipped with a gas outlet pipe, and the gas outlet pipe is equipped with a third gas sampling port. The patent uses a hydrolysis reactor to carry out hydrolysis reaction, and then uses a solution absorption tank to absorb sulfur-containing gas. The device and the method provided by the patent can well remove the hydrogen sulfide and the carbon dioxide, but have the problems of quick reduction of separation efficiency and incomplete separation in long-period operation, and have adverse effects on the operation stability, energy conservation, consumption reduction and safe and environment-friendly operation of the whole ethylene glycol production device.
Therefore, in order to realize the purpose of long-period operation of the production device and high-efficiency separation of carbon monoxide, carbon dioxide and hydrogen sulfide, a new gas separation system for carbon monoxide, carbon dioxide and hydrogen sulfide is urgently needed.
Disclosure of Invention
The utility model provides a system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide, which aims to effectively solve the problems of rapid reduction of separation efficiency and incomplete separation in long-period operation of the existing carbon monoxide, carbon dioxide and hydrogen sulfide separation device and ensure long-period safe, environment-friendly, efficient and energy-saving operation of a production device. The system has the advantages of simple process flow, high separation efficiency, realization of selective separation of carbon monoxide, carbon dioxide and hydrogen sulfide respectively, and stable long-period operation.
The utility model aims at realizing the following technical scheme: the system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide comprises an absorption tower I, a heat exchanger I, a gas-liquid separator I, a solution filtering device, a heat exchanger II, a heat exchanger III, a solution desalting device, a lean liquid pump, a solution pump, a semi-lean liquid pump, a normal Jie Qidi tower, a reboiler, a heat exchanger IV, a gas-liquid separator II, an absorption tower II, a desulfurizing tower, a rich liquid pump, a regeneration tank, a sulfur foam tank and a sulfur foam pump.
The top outlet of the absorption tower I is connected with the inlet of the heat exchanger I, the outlet of the heat exchanger I is connected with the lower inlet of the gas-liquid separator I, and the upper outlet of the gas-liquid separator I is connected with a device outside the system; the lower outlet of the absorption tower I is connected with the upper inlet of a normal stripping tower, the upper outlet of the normal stripping tower is connected with the inlet of a heat exchanger IV, the outlet of the heat exchanger IV is connected with the lower inlet of a gas-liquid separator II, the upper outlet of the gas-liquid separator II is connected with the top inlet of the absorption tower II, the middle outlet of the absorption tower II is connected with the lower inlet of a desulfurizing tower, and the upper outlet of the desulfurizing tower is connected with a device outside the system; the lower outlet of the absorption tower II is connected with the inlet of a rich liquid pump, the outlet of the rich liquid pump is connected with the upper inlet of a regeneration tank, the upper outlet of the regeneration tank is connected with the upper inlet of a sulfur foam tank, the lower outlet of the sulfur foam tank is connected with the inlet of a sulfur foam pump, and the sulfur foam pump is connected with a device outside the system; the lower outlet of the regeneration tank is connected with the inlet of a regeneration liquid pump, and the outlet of the regeneration liquid pump is connected with the upper inlet of the absorption tower II; the middle outlet of the normal Jie Qidi tower is respectively connected with the inlet of the semi-lean liquid pump and the inlet of the solution pump, and the outlet of the semi-lean liquid pump is connected with the middle inlet of the absorption tower I; the solution pump outlet is connected with the inlet of a heat exchanger II, and the outlet of the heat exchanger II is connected with the inlet in the middle of the normal stripping tower; the outlet of the bottom of the normal stripping tower is connected with the inlet of a heat exchanger II, the outlet of the heat exchanger II is connected with the inlet of a lean liquid pump, the outlet of the lean liquid pump is connected with the inlet of a heat exchanger III, and the outlet of the heat exchanger III is connected with the inlet of the upper part of an absorption tower I.
The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that a pipeline of an outlet of the heat exchanger II, which is connected with an inlet at the middle part of a normal Jie Qidi tower, is connected with a solution filtering device in parallel to filter solid impurities in the solution A.
The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide comprises the mechanical filter, the activated carbon filter and the precise filter which are sequentially connected, wherein the filtering precision of the mechanical filter is 25 mu m, and the filtering precision of the precise filter is 5 mu m.
The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that a solution desalting device is connected in parallel on a pipeline of an outlet of a heat exchanger II connected with an inlet of a lean solution pump, so that heat stable salt in the solution B is removed.
The solution desalting device comprises a cloth bag type filter and a resin tower which are sequentially connected, and the resin tower is filled with ion exchange resin.
The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that the heat exchanger I, the heat exchanger II, the heat exchanger III and the heat exchanger IV are shell-and-tube heat exchangers.
The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that the absorption tower I, the absorption tower II and the common Jie Qidi tower are all packed towers.
The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is adopted, and the efficient separation of the carbon monoxide, the carbon dioxide and the hydrogen sulfide is realized through the following steps:
(1) The mixed gas containing carbon monoxide, carbon dioxide, hydrogen sulfide and other components enters the absorption tower I from a gas phase inlet at the lower part of the absorption tower I, and sequentially contacts with a solution A entering the absorption tower I from a liquid phase inlet at the middle part of the absorption tower I and a solution B entering the absorption tower I from a liquid phase inlet at the upper part of the absorption tower I in a reverse way, and the carbon dioxide and the hydrogen sulfide in the mixed gas are absorbed by a solution A, B to form a gas-liquid mixture which enters the liquid phase inlet at the upper part of the normal stripping tower; carbon monoxide flows out from a gas phase outlet at the top of the absorption tower I, is cooled by the heat exchanger I, enters the gas-liquid separator I, separates trace moisture in the gas-liquid separator I, and is sent to a device outside the system;
(2) The gas-liquid mixture entering the normal stripping tower from the liquid phase inlet at the upper part of the normal stripping tower moves from top to bottom, carbon dioxide and hydrogen sulfide in the gas-liquid mixture are resolved, the carbon dioxide and hydrogen sulfide gas leave the normal Jie Qidi tower from the gas phase outlet at the upper part of the normal stripping tower and then enter the gas-liquid separator II after being cooled by the heat exchanger IV, trace moisture is separated in the gas-liquid separator II, then enters the absorption tower II from the gas phase inlet at the top of the absorption tower II, contacts with the solution C entering from the liquid phase inlet at the upper part of the absorption tower II in the same direction, and most of hydrogen sulfide in the mixed gas is absorbed by the solution C; carbon dioxide leaves the absorption tower II from a gas phase outlet in the middle of the absorption tower II, and is sent to a device outside the system after removing trace hydrogen sulfide by the desulfurization tower;
(3) The solution C absorbed with hydrogen sulfide flows out from a liquid phase outlet at the bottom of the absorption tower II, is pumped to a regeneration tank through a rich liquid pump, the hydrogen sulfide reacts with the solution C, the hydrogen sulfide is oxidized into elemental sulfur, and sulfur foam containing the elemental sulfur overflows from the upper part of the regeneration tank to a sulfur foam tank and is pumped to a device outside the system through the sulfur foam pump; the solution C after reacting with hydrogen sulfide reacts with oxygen in air entering through a gas phase inlet at the upper part of the regeneration tank to achieve the purpose of regenerating the solution C, and the regenerated solution C is pumped to a liquid phase inlet at the upper part of the absorption tower II through a regenerating liquid pump;
(4) The solution A in the normal Jie Qidi tower, which resolves most of carbon dioxide and hydrogen sulfide, flows out from a liquid phase outlet in the middle of the normal stripping tower in two ways, and one way is pumped to a liquid phase inlet in the middle of the absorption tower I through a semi-lean liquid pump; one path is pumped to the inlet of the heat exchanger II through a solution pump, and exchanges heat with the solution B which flows out from the liquid phase outlet at the bottom of the normal stripping tower and is analyzed with a small part of carbon dioxide and hydrogen sulfide in the heat exchanger II; the solution A after heat exchange is divided into two paths, one path is directly sent to a liquid phase inlet in the middle part of the normal stripping tower, and the other path is sent to the liquid phase inlet in the middle part of the normal stripping tower after solid impurities in the solution A are filtered by a solution filtering device;
(5) The solution B subjected to heat exchange in the heat exchanger II is divided into two paths, one path is directly sent to an inlet of a lean solution pump, and the other path is sent to the inlet of the lean solution pump after the heat stable salt in the solution is removed by a solution desalting device; and cooling the solution B at the outlet of the lean liquid pump by a heat exchanger III, and then entering the absorption tower I from a liquid phase inlet at the upper part of the absorption tower I.
The solution A in the step described above is an MDEA solution containing 15-30. Mu.L/L carbon dioxide.
The solution B in the above step is an MDEA solution containing 1-5. Mu.L/L carbon dioxide.
The method for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that the solution C is a complex iron solution.
In the above steps, when the ion exchange resin in the resin tower in the solution desalination device reaches the working exchange capacity, the solution with 3% -5% sodium hydroxide by mass fraction is required for backwashing and regeneration.
Compared with the prior art, the utility model has the advantages that: (1) Through innovative technological process, scientifically and reasonably set operating temperature and operating pressure, the efficient absorption of carbon dioxide and hydrogen sulfide gas by the absorption tower I and the efficient absorption of hydrogen sulfide gas by the absorption tower II are realized, and the beneficial effects of efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide are achieved by matching with the operation of the normal Jie Qidi tower. (2) The mixed gas is acid gas, and can corrode the packing in the absorption tower I and the normal stripping tower, and the packing scraps are brought into the solution after the packing corrosion, so that the content of solid impurities in the MDEA solution is increased, and the packing is blocked. (3) In the normal production process, the MDEA solution can react with other acidic compounds in the system to form heat stable salts besides absorbing carbon dioxide and hydrogen sulfide, and the heat stable salts are not easy to resolve under the stripping condition, and can cause solution foaming, filler corrosion and equipment corrosion, so that the consumption of the MDEA solution is increased. Therefore, the solution desalting device is arranged to remove the heat stable salt in the MDEA solution, so that the efficient recycling of the MDEA solution is realized, the economical efficiency of system operation is improved, and the beneficial effect of long-period stable operation is achieved.
Drawings
The accompanying drawings are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate the utility model and together with the embodiments of the utility model, serve to explain the utility model.
FIG. 1 is a process flow diagram of the present utility model.
FIG. 2 is a flow chart of a solution desalination apparatus of the present utility model.
FIG. 3 is a flow chart of the solution filtering device of the present utility model.
In fig. 1, 1 is an absorption tower i, 2 is a heat exchanger i, 3 is a gas-liquid separator i, 4 is a solution filtering device, 5 is a heat exchanger ii, 6 is a heat exchanger iii, 7 is a solution desalting device, 8 is a lean solution pump, 9 is a solution pump, 10 is a semi-lean solution pump, 11 is a normal stripping tower, 12 is a reboiler, 13 is a heat exchanger iv, 14 is a gas-liquid separator ii, 15 is an absorption tower ii, 16 is a desulfurizing tower, 17 is a rich solution pump, 18 is a regeneration liquid pump, 19 is a regeneration tank, 20 is a sulfur foam tank, and 21 is a sulfur foam pump.
Description of the embodiments
Referring to fig. 1, an embodiment of the utility model provides a system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide, which comprises an absorption tower I, a heat exchanger I, a gas-liquid separator I, a solution filtering device, a heat exchanger II, a heat exchanger III, a solution desalting device, a lean liquid pump, a solution pump, a semi-lean liquid pump, a normal Jie Qidi tower, a reboiler, a heat exchanger IV, a gas-liquid separator II, an absorption tower II, a desulfurizing tower, a rich liquid pump, a regeneration tank, a sulfur foam tank and a sulfur foam pump.
The top outlet of the absorption tower I is connected with the inlet of the heat exchanger I, the outlet of the heat exchanger I is connected with the lower inlet of the gas-liquid separator I, and the upper outlet of the gas-liquid separator I is connected with a device outside the system; the lower outlet of the absorption tower I is connected with the upper inlet of a normal stripping tower, the upper outlet of the normal stripping tower is connected with the inlet of a heat exchanger IV, the outlet of the heat exchanger IV is connected with the lower inlet of a gas-liquid separator II, the upper outlet of the gas-liquid separator II is connected with the top inlet of the absorption tower II, the middle outlet of the absorption tower II is connected with the lower inlet of a desulfurizing tower, and the upper outlet of the desulfurizing tower is connected with a device outside the system; the lower outlet of the absorption tower II is connected with the inlet of a rich liquid pump, the outlet of the rich liquid pump is connected with the upper inlet of a regeneration tank, the upper outlet of the regeneration tank is connected with the upper inlet of a sulfur foam tank, the lower outlet of the sulfur foam tank is connected with the inlet of a sulfur foam pump, and the sulfur foam pump is connected with a device outside the system; the lower outlet of the regeneration tank is connected with the inlet of a regeneration liquid pump, and the outlet of the regeneration liquid pump is connected with the upper inlet of the absorption tower II; the middle outlet of the normal Jie Qidi tower is respectively connected with the inlet of the semi-lean liquid pump and the inlet of the solution pump, and the outlet of the semi-lean liquid pump is connected with the middle inlet of the absorption tower I; the solution pump outlet is connected with the inlet of a heat exchanger II, and the outlet of the heat exchanger II is connected with the inlet in the middle of the normal stripping tower; the outlet of the bottom of the normal stripping tower is connected with the inlet of a heat exchanger II, the outlet of the heat exchanger II is connected with the inlet of a lean liquid pump, the outlet of the lean liquid pump is connected with the inlet of a heat exchanger III, and the outlet of the heat exchanger III is connected with the inlet of the upper part of an absorption tower I.
Another embodiment is different in that the system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that a solution filtering device is connected in parallel on a pipeline of which the outlet of the heat exchanger II is connected with the inlet of the middle part of the normal Jie Qidi tower, so as to filter solid impurities in the solution A.
Another embodiment is different in that the system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide comprises a mechanical filter, an activated carbon filter and a precision filter which are sequentially connected, wherein the filtering precision of the mechanical filter is 25 μm, and the filtering precision of the precision filter is 5 μm.
The other embodiment is different in that the system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that a solution desalting device is connected in parallel on a pipeline of which the outlet of the heat exchanger II is connected with the inlet of the lean solution pump, so that heat stable salt in the solution B is removed.
Another embodiment is different in that the system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide comprises a cloth bag filter and a resin tower which are sequentially connected, wherein the resin tower is filled with ion exchange resin.
The other embodiment is different in that the system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that the heat exchanger I, the heat exchanger II, the heat exchanger III and the heat exchanger IV are shell-and-tube heat exchangers.
The other embodiment is different in that the system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide is characterized in that the absorption tower I, the absorption tower II and the common Jie Qidi tower are all packed towers.
The foregoing description of the preferred embodiments of the utility model is not intended to limit the utility model to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the utility model are intended to be included within the scope of the utility model.
Claims (5)
1. System for high-efficient separation carbon monoxide, carbon dioxide, hydrogen sulfide, its characterized in that: the system comprises an absorption tower I, a heat exchanger I, a gas-liquid separator I, a solution filtering device, a heat exchanger II, a heat exchanger III, a solution desalting device, a lean liquid pump, a solution pump, a semi-lean liquid pump, a normal Jie Qidi tower, a reboiler, a heat exchanger IV, a gas-liquid separator II, an absorption tower II, a desulfurizing tower, a rich liquid pump, a regeneration tank, a sulfur foam tank and a sulfur foam pump;
The top outlet of the absorption tower I is connected with the inlet of the heat exchanger I, the outlet of the heat exchanger I is connected with the lower inlet of the gas-liquid separator I, and the upper outlet of the gas-liquid separator I is connected with a device outside the system; the lower outlet of the absorption tower I is connected with the upper inlet of a normal stripping tower, the upper outlet of the normal stripping tower is connected with the inlet of a heat exchanger IV, the outlet of the heat exchanger IV is connected with the lower inlet of a gas-liquid separator II, the upper outlet of the gas-liquid separator II is connected with the top inlet of the absorption tower II, the middle outlet of the absorption tower II is connected with the lower inlet of a desulfurizing tower, and the upper outlet of the desulfurizing tower is connected with a device outside the system; the lower outlet of the absorption tower II is connected with the inlet of a rich liquid pump, the outlet of the rich liquid pump is connected with the upper inlet of a regeneration tank, the upper outlet of the regeneration tank is connected with the upper inlet of a sulfur foam tank, the lower outlet of the sulfur foam tank is connected with the inlet of a sulfur foam pump, and the sulfur foam pump is connected with a device outside the system; the lower outlet of the regeneration tank is connected with the inlet of a regeneration liquid pump, and the outlet of the regeneration liquid pump is connected with the upper inlet of the absorption tower II; the middle outlet of the normal Jie Qidi tower is respectively connected with the inlet of the semi-lean liquid pump and the inlet of the solution pump, and the outlet of the semi-lean liquid pump is connected with the middle inlet of the absorption tower I; the solution pump outlet is connected with the inlet of a heat exchanger II, and the outlet of the heat exchanger II is connected with the inlet in the middle of the normal stripping tower; the outlet of the bottom of the normal stripping tower is connected with the inlet of a heat exchanger II, the outlet of the heat exchanger II is connected with the inlet of a lean liquid pump, the outlet of the lean liquid pump is connected with the inlet of a heat exchanger III, and the outlet of the heat exchanger III is connected with the inlet of the upper part of an absorption tower I.
2. The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide according to claim 1, wherein: the solution filtering device is connected in parallel to a pipeline of an inlet in the middle of a normal Jie Qidi tower connected with an outlet of the heat exchanger II, and comprises a mechanical filter, an activated carbon filter and a precision filter which are sequentially connected, wherein the filtering precision of the mechanical filter is 25 mu m, and the filtering precision of the precision filter is 5 mu m.
3. The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide according to claim 1, wherein: the solution desalting device is connected in parallel to a pipeline of the outlet of the heat exchanger II connected with the inlet of the lean solution pump, and comprises a cloth bag filter and a resin tower which are sequentially connected, wherein the resin tower is filled with ion exchange resin.
4. The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide according to claim 1, wherein: the heat exchanger I, the heat exchanger II, the heat exchanger III and the heat exchanger IV are shell-and-tube heat exchangers.
5. The system for efficiently separating carbon monoxide, carbon dioxide and hydrogen sulfide according to claim 1, wherein: the absorption tower I, the absorption tower II and the normal Jie Qidi tower are all packed towers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323421697.3U CN221619022U (en) | 2023-12-15 | 2023-12-15 | System for high-efficient separation carbon monoxide, carbon dioxide and hydrogen sulfide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323421697.3U CN221619022U (en) | 2023-12-15 | 2023-12-15 | System for high-efficient separation carbon monoxide, carbon dioxide and hydrogen sulfide |
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| Publication Number | Publication Date |
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| CN221619022U true CN221619022U (en) | 2024-08-30 |
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| CN202323421697.3U Active CN221619022U (en) | 2023-12-15 | 2023-12-15 | System for high-efficient separation carbon monoxide, carbon dioxide and hydrogen sulfide |
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| Country | Link |
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| CN (1) | CN221619022U (en) |
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