CN110548370A - Acid gas purification process and device for producing hydrogen sulfide with various purities - Google Patents
Acid gas purification process and device for producing hydrogen sulfide with various purities Download PDFInfo
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- CN110548370A CN110548370A CN201910831878.2A CN201910831878A CN110548370A CN 110548370 A CN110548370 A CN 110548370A CN 201910831878 A CN201910831878 A CN 201910831878A CN 110548370 A CN110548370 A CN 110548370A
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- 239000007789 gas Substances 0.000 title claims abstract description 123
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 229910000037 hydrogen sulfide Inorganic materials 0.000 title claims abstract description 65
- 239000002253 acid Substances 0.000 title claims abstract description 43
- 238000000746 purification Methods 0.000 title claims abstract description 31
- 238000003795 desorption Methods 0.000 claims abstract description 166
- 239000002904 solvent Substances 0.000 claims abstract description 103
- 238000000034 method Methods 0.000 claims abstract description 51
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 39
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000011593 sulfur Substances 0.000 claims abstract description 36
- 238000010521 absorption reaction Methods 0.000 claims description 61
- 239000000463 material Substances 0.000 claims description 40
- 238000010992 reflux Methods 0.000 claims description 40
- 239000012071 phase Substances 0.000 claims description 27
- 239000007791 liquid phase Substances 0.000 claims description 23
- 238000011084 recovery Methods 0.000 claims description 20
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 claims description 7
- 238000005265 energy consumption Methods 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 6
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 claims description 3
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 claims description 3
- 229940043276 diisopropanolamine Drugs 0.000 claims description 3
- 239000002737 fuel gas Substances 0.000 claims description 3
- 239000000126 substance Substances 0.000 abstract description 10
- 238000011161 development Methods 0.000 abstract description 2
- UMGDCJDMYOKAJW-UHFFFAOYSA-N thiourea Chemical compound NC(N)=S UMGDCJDMYOKAJW-UHFFFAOYSA-N 0.000 description 14
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Natural products NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 7
- 239000002994 raw material Substances 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000005457 optimization Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 101100348341 Caenorhabditis elegans gas-1 gene Proteins 0.000 description 1
- 101100447658 Mus musculus Gas1 gene Proteins 0.000 description 1
- 101100447665 Mus musculus Gas2 gene Proteins 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000012938 design process Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052979 sodium sulfide Inorganic materials 0.000 description 1
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
the invention provides an acid gas purification process and a device for producing hydrogen sulfide with various purities, because of the development of downstream product processes of different H 2 S and different requirements of various sulfur chemicals on the purity of H 2 S gas, the invention utilizes the solubility difference of H 2 S and CO 2 in a solvent and adopts an absorption-step desorption mode to obtain H 2 S gas with different purities.
Description
Technical Field
The invention relates to a desulfurization purification device for producing acid gas in the production processes of petrochemical industry, coal chemical industry, natural gas industry and the like, in particular to a purification process and a purification device for producing hydrogen sulfide with various purities for acid gas.
background
The sulfur-containing acid gas mainly comes from natural gas exploitation, oilfield associated gas, coal chemical industry and petrochemical industry, impurities of the sulfur-containing acid gas mainly include H 2 S, CO 2 and the like, steel pipelines, equipment and burners are corroded, the service life of the sulfur-containing acid gas is shortened, meanwhile, sulfur in process gas can poison catalysts and damage the normal operation of the process, and therefore the sulfur-containing acid gas needs to be removed to reach the emission standard of each gas.
the existing acid gas purification device adopts an absorption-desorption method (see figure 1), sulfur-containing acid gas firstly enters the bottom of an absorption tower and is in multi-stage countercurrent contact with desorbed lean solvent, desulfurized purified gas is taken at the tower top and is sent out after entrained liquid drops are separated by a purification gas separator, rich solvent is taken at the tower bottom, hydrocarbons are flashed under reduced pressure by a flash tank, then the hydrocarbons are heated by a lean-rich solvent heat exchanger and enter a desorption tower, an H 2 S gas desulphurization recovery device is obtained at the desorption tower top, the lean solvent at the desorption tower bottom sequentially passes through the lean-rich solvent heat exchanger, is pressurized and cooled by water and then returns to the absorption tower top, H 2 S gas obtained by desorption has lower purity, the downstream sulfur recovery device is single, generally is a sulfur device and has low added value, but along with the increase of sulfur content in fossil fuels such as crude oil and the like and the continuous development of processes for producing high added-value sulfur chemicals (such as a sodium sulfide process, a thiourea process and the like), how to better provide and utilize H 2 S resources.
Patent CN 1088472a provides a method for removing carbon dioxide from a mixed gas, which adopts a flow of two-stage absorption and two-stage desorption, and reduces the energy consumption of a desorption tower by extracting a lean solvent and a semi-lean solvent.
The patent CN 103446849a provides a technology for separating high-purity H 2 S from acid gas, the acid gas firstly enters a first absorption tower and a first regeneration tower, the regenerated gas enters a second absorption tower and a second regeneration tower, and finally high-purity H 2 S gas is obtained, which is essentially the coupling of two sets of absorption-desorption systems, and high-purity H 2 S gas is obtained through multiple absorption-desorption operations.
patent CN 101054167A provides a separation process of high-purity H 2 S, NHD solvent is adopted for absorption, the obtained rich solvent is subjected to multistage flash evaporation, each flash evaporation gas returns to an absorption tower, the finally flashed liquid phase enters a desorption tower, and high-purity H 2 S gas is obtained, and the essence of the high-purity H 2 S gas is that the purity of the H 2 S gas is improved in a mode of recycling regeneration gas and absorbing for multiple times.
patent CN 108392948A provides a process and an apparatus for purifying hydrogen sulfide, which are used for purifying crude hydrogen sulfide gas obtained from an upstream apparatus, such as an acid gas purification apparatus, to high-purity hydrogen sulfide gas by means of multi-stage pressure swing adsorption.
The patent US 2008127831a1 provides a technology for multi-stage desorption after absorbing CO 2 gas, which mainly considers that the operation pressure of a downstream CO 2 recovery device is higher, and a one-step desorption mode is adopted, so that the pressure of CO 2 gas is lower, and the compression power consumption of the gas going to the downstream device is increased, and therefore, the comprehensive optimization of the compression power consumption and the energy consumption of a desorption tower is achieved by configuring multiple stages of desorption towers with different pressures.
at present, all patents related to acid gas purification devices are technologies for saving energy and reducing consumption or improving the purity of H 2 S gas, which are provided aiming at a single downstream recovery device.
Disclosure of Invention
The invention relates to an acid gas purification process and a device for producing hydrogen sulfide with various purities, wherein the conventional process adopts a method of single-tower absorption and single-tower desorption (see figure 1), the obtained H 2 S gas generally enters a downstream sulfur device for recycling, the added value of the product is low, and the two most main factors in the whole acid gas purification device, namely the purity of a lean solvent and the content of impurities in the solvent, are limited by the low added value of the downstream product in the conventional process, so that the optimization of the main factors firstly considers the energy consumption of the device and secondly considers the selectivity of the solvent, and the process design of the device is carried out.
Compared with the conventional process, the invention takes different sulfur chemicals as guidance, utilizes the solubility difference of acid gas components (CO 2, H 2 S and the like) in a solvent, namely the solubility of CO 2 is lower than that of H 2 S, and CO 2 is preferentially desorbed in the desorption process, so that each H 2 S gas with high purity is sequentially obtained by adopting a step-by-step desorption mode.
Meanwhile, in order to obtain more high-purity H 2 S gas, the absorption amount of CO 2 needs to be reduced in the absorption process, namely the selectivity of the solvent to H 2 S is improved, so that compared with the conventional design, the process design of the product-oriented acid gas purification device has more prominent influence on the selectivity of the solvent, the yield of the high-purity hydrogen sulfide is directly determined, and two factors of the energy consumption of the device and the selectivity of the solvent are considered simultaneously in the process design process of selecting parameters.
In the design of the absorption tower, the absorption of H 2 S is faster than that of CO 2, so that the solvent selectivity can be improved by reducing the gas-liquid phase contact time in the tower (such as reducing the diameter of the tower), and the like.
The technical scheme of the invention is as follows:
An acid gas purification device for producing hydrogen sulfide with various purities comprises an absorption tower, a flash tank 3, a lean rich solvent heat exchanger 4, a lean solvent pump 5, a lean solvent cooler 6, a desorption tower condenser, a desorption tower reflux tank, a desorption tower reflux pump, a desorption tower reboiler and a desorption tower bottom semi-lean solvent pump;
the top of the absorption tower is a gas phase outlet which is connected with a downstream device; the tower bottom of the common absorption tower 1 or the reducing absorption tower 2 is a liquid phase outlet which is connected with a flash tank 3; when the absorption tower is a common absorption tower 1, a stream of sour gas containing sulfur enters from the gas inlet; when the absorption tower is a reducing absorption tower 2, two sulfur-containing acid gases respectively enter from corresponding air inlets; the top of the flash tank 3 is a gas phase outlet, and flash gas is connected with a fuel gas pipe network; the bottom of the flash tank 3 is a liquid phase outlet which is connected with a cold material flow inlet of the lean-rich solvent heat exchanger 4, a cold material flow outlet of the lean-rich solvent heat exchanger 4 is connected with a feed inlet of a first desorption tower 7, a gas phase outlet at the top of the first desorption tower 7 is connected with a process material flow inlet of a first desorption tower condenser 8, a process material flow outlet of the first desorption tower condenser 8 is connected with an inlet of a first desorption tower reflux tank 9, a liquid phase outlet of the first desorption tower reflux tank 9 is connected with an inlet of a first desorption tower reflux pump 10, and a gas phase outlet of the first desorption tower reflux tank 9 is connected with a downstream hydrogen sulfide recovery device; the outlet of a first desorption tower reflux pump 10 is connected with a reflux port of a first desorption tower 7, a liquid phase outlet at the bottom of the first desorption tower 7 is divided into two branches, one branch is connected with a process material flow inlet of a first desorption tower reboiler 11, and a process material flow outlet of the first desorption tower reboiler 11 is connected with a reflux port at the bottom of the first desorption tower 7; the other branch is connected with the inlet of a first desorption tower bottom semi-lean solvent pump 12, the outlet of the first desorption tower bottom semi-lean solvent pump 12 is connected with the inlet of a second desorption tower 13, and the matching equipment and the connection mode of the second desorption tower 13 are the same as those of the first desorption tower 7;
When two desorption towers exist in the acid gas purification device, the gas phase outlet of the first desorption tower reflux tank 9 is connected with a downstream low-concentration/medium-concentration hydrogen sulfide recovery device, and the gas phase outlet of the second desorption tower reflux tank 15 is connected with the downstream medium-concentration/high-concentration hydrogen sulfide recovery device; a tower bottom liquid phase outlet of the second desorption tower 13 is connected with a hot material flow inlet of the lean-rich solvent heat exchanger 4, a hot material flow outlet of the lean-rich solvent heat exchanger 4 is connected with an inlet of the lean solvent pump 5, an outlet of the lean solvent pump 5 is connected with a process material flow inlet of the lean solvent cooler 6, and a process material flow outlet of the lean solvent cooler 6 is connected with a liquid phase feeding port of the absorption tower;
When three desorption towers exist in the acid gas purification device, the matching equipment and the connection mode of the third desorption tower 19 are the same as those of the first desorption tower 7; a gas phase outlet of the first desorption tower reflux tank 9 is connected with a downstream low-concentration hydrogen sulfide recovery device, a gas phase outlet of the second desorption tower reflux tank 15 is connected with a downstream medium-concentration hydrogen sulfide recovery device, and a gas phase outlet of the third desorption tower reflux tank is connected with a downstream high-concentration hydrogen sulfide recovery device; the tower bottom liquid phase outlet of the second desorption tower 13 is connected with the hot material flow inlet of the lean-rich solvent heat exchanger 4, the hot material flow outlet of the lean-rich solvent heat exchanger 4 is connected with the inlet of the lean solvent pump 5, the outlet of the lean solvent pump 5 is connected with the process material flow inlet of the lean solvent cooler 6, and the process material flow outlet of the lean solvent cooler 6 is connected with the liquid phase feeding hole of the absorption tower.
An acid gas purification process for producing hydrogen sulfide with various purities comprises the following steps:
(1) One or two streams of sour gas containing sulfur enter an acid gas purification device, and firstly enter an absorption tower, and when one stream of feed is fed, the sour gas containing sulfur directly enters the bottom of a common absorption tower 1; when two strands of materials are fed, different feeding ports are arranged, and the solvent selectivity is further improved by adopting a reducing absorption tower 2 mode according to the hydraulics condition among the feeding ports and on the premise of the permission of equipment design;
(2) the lean solvent enters the top of the absorption tower to ensure that the sulfur content in the purified gas at the top of the absorption tower reaches the standard, the purity and the impurity content of the lean solvent are comprehensively determined according to the energy consumption of a device and the selectivity of the solvent, and the selectivity of the solvent is preferably considered in order to obtain more high-purity hydrogen sulfide;
(3) The rich solvent at the bottom of the tower sequentially passes through a flash tank 3 to flash evaporate partial light hydrocarbon, and is heated by a lean and rich solvent heat exchanger 4, the temperature difference at the 4 end of the lean and rich solvent heat exchanger is selected to be 10-15 ℃, and the lean and rich solvent enters a desorption unit after heat exchange;
(4) The desorption unit is provided with two to three desorption towers, and respectively desorbs and sucks hydrogen sulfide gas with different purities, namely H 2 S is more than or equal to 95% of high-purity hydrogen sulfide gas, H 2 S is 85% -95% of medium-purity hydrogen sulfide gas and H 2 S is 70% -85% of low-purity hydrogen sulfide gas;
(5) The lean solvent is obtained at the bottom of the last stage desorption tower, and enters the top of the absorption tower after being sequentially cooled by a lean rich solvent heat exchanger 4, pressurized by a lean solvent pump 5 and cooled by a lean solvent cooler 6.
In the step (2), the solvent type for absorption should be selected from one or More of Ethanolamine (MEA), Diethanolamine (DEA), Methyldiethanolamine (MDEA) and Diisopropanolamine (DIPA), and preferably Methyldiethanolamine (MDEA), wherein the solubility of H 2 S is better than that of CO 2.
The invention has the beneficial effects that: the invention provides the acid gas purification process and the device for producing hydrogen sulfide with various purities based on the requirements of different hydrogen sulfide purities required by different sulfur chemicals.
Drawings
fig. 1 is a process diagram of a conventional acid gas purification device.
FIG. 2 is a process diagram of the acid gas purification apparatus of the present invention: the absorption tower is fed with single sulfur-containing acidic gas, the desorption unit comprises two desorption towers, and the first desorption tower and the second desorption tower can extract low-purity and medium-purity hydrogen sulfide, low-purity and high-purity hydrogen sulfide and medium-purity and high-purity hydrogen sulfide.
FIG. 3 is a process diagram of the acid gas purification apparatus of the present invention: the absorption tower is fed with single-stranded sulfur-containing acidic gas, the desorption unit comprises three desorption towers, and the first desorption tower, the second desorption tower and the third desorption tower respectively extract low-purity, medium-purity and high-purity hydrogen sulfide.
FIG. 4 is a process diagram of the acid gas purification apparatus of the present invention: the absorption tower is provided with a plurality of sulfur-containing acid gas feeds (taking two as an example), the desorption unit comprises two desorption towers, and the first desorption tower and the second desorption tower can produce low-purity and medium-purity hydrogen sulfide, low-purity and high-purity hydrogen sulfide and medium-purity and high-purity hydrogen sulfide.
FIG. 5 is a process diagram of the acid gas purification apparatus of the present invention: the absorption tower is provided with a plurality of sulfur-containing acid gas feeds (taking two strands as an example), the desorption unit comprises three desorption towers, and the first desorption tower, the second desorption tower and the third desorption tower respectively extract hydrogen sulfide with low purity, medium purity and high purity.
in the figure: 1, a common absorption tower; 2, a reducing absorption tower; 3, a flash tank; 4 lean-rich solvent heat exchanger; 5 a lean solvent pump; 6 lean solvent cooler; 7a first desorber; 8a first desorber condenser; 9a first desorber reflux drum; 10 a first desorber reflux pump; 11 a first desorber reboiler; 12 a first stripper bottoms semi-lean solvent pump; 13 a second desorber; 14 a second desorber condenser; 15 a second desorber reflux drum; 16 a second desorber reflux pump; 17 a second desorber reboiler; 18 a second stripper bottoms semi-lean solvent pump; 19 a third desorber; 20 a third desorber condenser; 21 a third desorber reflux drum; 22 a third stripper reflux pump; 23 third desorber reboiler.
Detailed Description
The technical solutions of the present invention will be described clearly and completely below, and it should be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments modified or wetted by those skilled in the art based on the embodiments of the present invention belong to the protection scope of the present invention.
When the absorption tower is single-stranded gas phase feeding, and according to the purity requirement and economic benefit of downstream sulfur chemicals, the desorption unit is obtained by adopting two desorption towers, the first desorption tower adopts hydrogen sulfide with lower purity, the second desorption tower adopts hydrogen sulfide with higher purity, namely, three conditions are adopted: the low-purity and medium-purity hydrogen sulfide is sequentially extracted, the low-purity and high-purity hydrogen sulfide is sequentially extracted, and the medium-purity and high-purity hydrogen sulfide is sequentially extracted, which is shown in figure 2.
When the absorption tower is fed in a single-stranded gas phase, and according to the purity requirement and economic benefit of downstream sulfur chemicals, the desorption unit adopts three desorption towers, wherein the first desorption tower adopts low-purity hydrogen sulfide, the second desorption tower adopts medium-purity hydrogen sulfide, and the third desorption tower adopts high-purity hydrogen sulfide, as shown in figure 3.
When the absorption tower is fed by a plurality of gas phases (taking two streams as an example), and according to the purity requirement and economic benefit of downstream sulfur chemicals, two desorption towers are adopted in the desorption unit, the first desorption tower produces hydrogen sulfide with lower purity, and the second desorption tower produces hydrogen sulfide with higher purity, namely, three cases are divided: the low-purity and medium-purity hydrogen sulfide is sequentially extracted, the low-purity and high-purity hydrogen sulfide is sequentially extracted, and the medium-purity and high-purity hydrogen sulfide is sequentially extracted, which is shown in figure 4.
when the absorption tower is fed by single-strand gas phase (taking two strands as an example), and according to the purity requirement and economic benefit of downstream sulfur chemicals, three desorption towers are adopted in the desorption unit, wherein the first desorption tower produces low-purity hydrogen sulfide, the second desorption tower produces medium-purity hydrogen sulfide, and the third desorption tower produces high-purity hydrogen sulfide, as shown in figure 5.
the method is explained in detail by using a plurality of strands of feed materials of the absorption tower and three desorption towers as desorption units:
The acid gas purification device for producing hydrogen sulfide with various purities provided by the invention is described by taking fig. 5 as an example:
The sulfur-containing acid gas-1 and the sulfur-containing acid gas-2 respectively enter different feed inlets of a reducing absorption tower 2 of an acid gas purification device, a tower top gas phase outlet is connected with a downstream device, a tower bottom liquid phase outlet is connected with a flash tank 3, the flash tank 3 gas phase outlet is connected with a fuel gas pipe network, the flash tank 3 liquid phase outlet is connected with a lean and rich solvent heat exchanger 4 cold material flow inlet, the lean and rich solvent heat exchanger 4 cold material flow outlet is connected with a first desorption tower 7 feed inlet, the tower top gas phase outlet of a first desorption tower 7 is connected with a first desorption tower condenser 8 process material flow inlet, the first desorption tower condenser 8 process material flow outlet is connected with a first desorption tower reflux tank 9 inlet, the first desorption tower reflux tank 9 liquid phase outlet is connected with a first desorption tower reflux pump 10 inlet, the first desorption tower reflux pump 10 gas phase outlet is connected with a downstream low-purity hydrogen sulfide recovery device, the first desorption tower reflux pump, the bottom liquid phase outlet of the first desorption tower 7 is divided into two branches, one branch is connected with the process material flow inlet of a first desorption tower reboiler 11, the process material flow outlet of the first desorption tower reboiler 11 is connected with the bottom reflux inlet of the first desorption tower 7, the other branch is connected with the inlet of a first desorption tower bottom semi-lean solvent pump 12, the outlet of the first desorption tower bottom semi-lean solvent pump 12 is connected with the inlet of a second desorption tower 13, the matching equipment and the connection mode of the second desorption tower 13 and a third desorption tower 19 are the same as those of the first desorption tower 7, the purity and high purity hydrogen sulfide in the tower top are sent to a corresponding sulfur recovery device, the bottom liquid phase outlet of the third desorption tower 19 is connected with the hot material flow inlet of a lean rich solvent heat exchanger 4, the hot material flow outlet of the lean rich solvent heat exchanger 4 is connected with the inlet of a lean solvent pump 5, the outlet of the lean solvent pump 5 is connected with the process material flow.
Example 1:
a petrochemical company has two catalytic dry gases (the feeding information is shown in table 1), the conventional absorption-desorption process is adopted in the original design, the two catalytic dry gases are mixed and enter the bottom of an absorption tower, a MDEA solution (subscript w is the mass fraction, m is the mole fraction and the like) with the impurity content of 40% w and 0.06% w is adopted, the H 2 S content in purified gas at the top of the tower is ensured to be lower than 20ppm v, the solvent consumption is 35400kg/H, the H 2 S gas purity is 88.92% m (dry basis content and the like) obtained at the top of a desorption tower, the petrochemical company has three sets of sulfur recovery devices which are respectively a NaHS device, a thiourea device and a sulfuric acid device, the product information is shown in table 2, and the H 2 S gas which is originally designed is completely introduced into the thiourea device according to the raw material purity.
according to the design method (the process flow is shown in figure 4), two catalytic dry gases enter different feed inlets according to the composition optimization, the tower diameter of each section of an absorption tower is optimized according to the gas phase quantity in the tower, the absorption tower adopts a variable diameter tower, a poor solvent adopts MDEA solution with 30 percent of w and 0.04 percent of w of impurity content, the consumption of the poor solvent is 39150kg/H on the premise of ensuring the desulfurization effect, if a direct desorption mode is adopted, 90.48 percent of m H 2 S gas can be obtained, the solvent selectivity is improved, the desorption unit is comprehensively optimized according to the raw material requirements, economic benefits and the like of a downstream recovery device, finally two desorption towers are matched, the tower pressure of a first desorption tower is 0.17MPa (gauge pressure, the same is carried out later), an 85 percent m H 2 S gas thiourea removal device is obtained, the tower pressure of a second desorption tower is 0.05MPa, and a 95 percent m H 2 S gas NaHS removal device is obtained.
The detailed information of the two designs is shown in a table 3, 58.58 kmol/H88.92% m H 2 S gas is obtained by the original design, the purity can only reach the raw material requirement of a thiourea device, 24.82 kmol/H85.18% m H 2 S gas can be obtained as the raw material of the thiourea device, 32.67 kmol/H95.01% m H 2 S gas is used as the raw material of a NaHS device by adopting a step-by-step desorption mode according to the design method, and the added value of the product is greatly improved compared with the original design.
TABLE 1
TABLE 2
TABLE 3
example 2:
On the basis of example 1, three-tower desorption flow is adopted to respectively obtain high-purity, medium-purity and low-purity hydrogen sulfide, as shown in fig. 5, the tower pressure of a first desorption tower is 0.45MPa, the tower pressure of a second desorption tower is 0.18MPa, and the tower pressure of a third desorption tower is 0.05 MPa. two designs of detailed information are shown in table 4, 58.58 kmol/H88.92% m H 2 S gas is obtained in the original design, and the purity can only reach the raw material requirement of a thiourea device.
TABLE 4
While only the preferred embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention.
Claims (4)
1. the acid gas purification device for producing the hydrogen sulfide with various purities is characterized by comprising an absorption tower, a flash tank (3), a lean rich solvent heat exchanger (4), a lean solvent pump (5), a lean solvent cooler (6), a desorption tower condenser, a desorption tower reflux tank, a desorption tower reflux pump, a desorption tower reboiler and a desorption tower bottom semi-lean solvent pump;
The top of the absorption tower is a gas phase outlet which is connected with a downstream device; the tower bottom of the common absorption tower (1) or the reducing absorption tower (2) is a liquid phase outlet which is connected with the flash tank (3); when the absorption tower is a common absorption tower (1), a stream of sour gas containing sulfur enters from the air inlet; when the absorption tower is a reducing absorption tower (2), two sulfur-containing acid gases respectively enter from corresponding air inlets; the top of the flash tank (3) is a gas phase outlet, and flash gas is connected with a fuel gas pipe network; the bottom of the flash tank (3) is a liquid phase outlet which is connected with a cold material flow inlet of the lean-rich solvent heat exchanger (4), a cold material flow outlet of the lean-rich solvent heat exchanger (4) is connected with a feed inlet of a first desorption tower (7), a gas phase outlet at the top of the first desorption tower (7) is connected with a process material flow inlet of a first desorption tower condenser (8), a process material flow outlet of the first desorption tower condenser (8) is connected with an inlet of a first desorption tower reflux tank (9), a liquid phase outlet of the first desorption tower reflux tank (9) is connected with an inlet of a first desorption tower reflux pump (10), and a gas phase outlet of the first desorption tower reflux tank (9) is connected with a downstream hydrogen sulfide recovery device; the outlet of a first desorption tower reflux pump (10) is connected with a reflux port of a first desorption tower (7), a liquid phase outlet at the bottom of the first desorption tower (7) is divided into two branches, one branch is connected with a process material flow inlet of a first desorption tower reboiler (11), and a process material flow outlet of the first desorption tower reboiler (11) is connected with the reflux port at the bottom of the first desorption tower (7); the other branch is connected with the inlet of a first desorption tower bottom semi-lean solvent pump (12), the outlet of the first desorption tower bottom semi-lean solvent pump (12) is connected with the inlet of a second desorption tower (13), and the matching equipment and the connection mode of the second desorption tower (13) are the same as those of the first desorption tower (7);
When two desorption towers exist in the acid gas purification device, a gas phase outlet of a reflux tank (9) of the first desorption tower is connected with a downstream low-concentration/medium-concentration hydrogen sulfide recovery device, and a gas phase outlet of a reflux tank (15) of the second desorption tower is connected with the downstream medium-concentration/high-concentration hydrogen sulfide recovery device; a tower bottom liquid phase outlet of the second desorption tower (13) is connected with a hot material flow inlet of the lean-rich solvent heat exchanger (4), a hot material flow outlet of the lean-rich solvent heat exchanger (4) is connected with an inlet of a lean solvent pump (5), an outlet of the lean solvent pump (5) is connected with a process material flow inlet of a lean solvent cooler (6), and a process material flow outlet of the lean solvent cooler (6) is connected with a liquid phase feeding port of the absorption tower;
When three desorption towers exist in the acid gas purification device, the matching equipment and the connection mode of the third desorption tower (19) are the same as those of the first desorption tower (7); a gas phase outlet of a reflux tank (9) of the first desorption tower is connected with a low-concentration hydrogen sulfide recovery device at the downstream, a gas phase outlet of a reflux tank (15) of the second desorption tower is connected with a medium-concentration hydrogen sulfide recovery device at the downstream, and a gas phase outlet of a reflux tank of the third desorption tower is connected with a high-concentration hydrogen sulfide recovery device at the downstream; the tower bottom liquid phase outlet of the second desorption tower (13) is connected with the hot material flow inlet of the lean-rich solvent heat exchanger (4), the hot material flow outlet of the lean-rich solvent heat exchanger (4) is connected with the inlet of the lean solvent pump (5), the outlet of the lean solvent pump (5) is connected with the process material flow inlet of the lean solvent cooler (6), and the process material flow outlet of the lean solvent cooler (6) is connected with the liquid phase feeding port of the absorption tower.
2. the acid gas purification process for producing hydrogen sulfide with various purities is characterized by comprising the following steps:
(1) One or two streams of sour gas containing sulfur enter an acid gas purification device, and firstly enter an absorption tower, and when one stream of sour gas containing sulfur directly enters the bottom of a common absorption tower (1); when two strands of materials are fed, different feeding ports are arranged, and the solvent selectivity is further improved by adopting a reducing absorption tower (2) mode according to the hydraulics condition among the feeding ports and on the premise of the permission of equipment design;
(2) The lean solvent enters the top of the absorption tower to ensure that the sulfur content in the purified gas at the top of the absorption tower reaches the standard, the purity and the impurity content of the lean solvent are comprehensively determined according to the energy consumption of a device and the selectivity of the solvent, and the selectivity of the solvent is preferably considered in order to obtain more high-purity hydrogen sulfide;
(3) The rich solvent at the bottom of the tower is sequentially subjected to flash evaporation to obtain partial light hydrocarbon through a flash evaporation tank (3), the light hydrocarbon is heated through a lean and rich solvent heat exchanger (4), the temperature difference at the end of the lean and rich solvent heat exchanger (4) is selected to be 10-15 ℃, and the light hydrocarbon enters a desorption unit after heat exchange;
(4) The desorption unit is provided with two to three desorption towers, and respectively desorbs and sucks hydrogen sulfide gas with different purities, namely H 2 S is more than or equal to 95% of high-purity hydrogen sulfide gas, H 2 S is 85% -95% of medium-purity hydrogen sulfide gas and H 2 S is 70% -85% of low-purity hydrogen sulfide gas;
(5) And the lean solvent obtained at the bottom of the last stage desorption tower enters the top of the absorption tower after being cooled by a lean rich solvent heat exchanger (4), pressurized by a lean solvent pump (5) and cooled by a lean solvent cooler (6) in sequence.
3. The process of claim 2, wherein the molar ratio of H 2 S to CO 2 in the sour gas is greater than 0.5.
4. The process of claim 2 or 3, wherein in step (2), the solvent type used for absorption is selected from one or more of ethanolamine, diethanolamine, methyldiethanolamine, and diisopropanolamine, and the solvent type has a solubility of H 2 S higher than that of CO 2.
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Cited By (1)
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