CN210645772U - Produce acid gas purifier of multiple purity hydrogen sulfide - Google Patents
Produce acid gas purifier of multiple purity hydrogen sulfide Download PDFInfo
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Abstract
The utility model provides an acid gas purification device for producing hydrogen sulfide with various purities, which is characterized in that different H's are used2S development of downstream product Process, and sulfur chemical Pair H2The S gas has different purity requirements, the utility model discloses utilize H2S and CO2The difference of solubility in the solvent adopts an absorption-fractional desorption mode to obtain H with different purities2And (4) S gas. The process can be provided with different numbers of desorption towers according to the requirements of a downstream sulfur recovery device to obtain H with various purities2S gas, and H gas can be regulated and controlled by regulating the pressure of each desorption tower2The purity of the S gas. The process provided by the utility model has the characteristics of simple operation, flexibility, low cost, strong adaptability to market, and the like.
Description
Technical Field
The utility model relates to a desulfurization purifier who produces acid gas in production processes such as petrochemical, coal chemical industry and natural gas industry, concretely relates to produce acid gas purifier of multiple purity hydrogen sulfide.
Background
The sulfur-containing acid gas mainly comes from natural gas exploitation, oilfield associated gas, coal chemical industry and petrochemical industry, and the impurities mainly comprise H2S and CO2And the like, the steel pipelines, equipment and burners are corroded, the service life of the steel pipelines, the equipment and the burners is shortened, and meanwhile, sulfur in the process gas can poison the catalyst and damage the normal operation of the process, so that the removal is required to reach the emission standard of each gas. At present, the treatment H is carried out at home and abroad2The methods of S gas can be divided into two broad categories: dry desulfurization and wet desulfurization. Dry desulfurization is mainly an adsorption method, wet desulfurization is mainly an absorption method, and the absorption process is widely applied due to the advantages of large treatment capacity, good purification effect and the like, wherein the absorption is divided into physical absorption and chemical absorption, common physical solvents comprise sulfolane, methanol and the like, and chemical solvents mainly comprise alcohol amine solvents, namely Monoethanolamine (MEA), Diethanolamine (DEA), Methyldiethanolamine (MDEA), Diisopropanolamine (DIPA) and the like. Each solvent is H2S and CO2The absorption effect of (2) is different, and the application scenes are also all different.
The prior 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 a desorbed lean solvent, desulfurized purified gas is taken at the top of the tower, entrained liquid drops are separated by a purification gas separator and then sent out, a rich solvent is taken at the bottom of the tower, hydrocarbons are firstly flashed out by reducing pressure of a flash tank, then the hydrocarbons are heated by a lean rich solvent heat exchanger and then enter a desorption tower, H is obtained at the top of the desorption tower2And in the S gas desulfurization recovery device, the lean solvent at the bottom of the desorption tower returns to the top of the absorption tower after sequentially passing through a lean rich solvent heat exchanger, pressurization and water cooling. H obtained by desorption2The purity of S gas is often lower, a downstream sulfur recovery device is single, a sulfur device is generally adopted, the added value of products is low, and stones such as crude oil and the like are generated along with the sulfur recovery deviceThe increasing of sulfur content in fuel and the continuous development of the process (such as sodium hydrosulfide process, thiourea process and the like) for producing high value-added sulfur chemicals, how to better provide and utilize H2S resources are the development direction of future acid gas purification devices.
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.
Patent CN 103446849A provides a method for separating high-purity H from acid gas2The S technology comprises the steps that acid gas firstly enters a first absorption tower and a first regeneration tower, gas obtained by regeneration enters a second absorption tower and a second regeneration tower, and high-purity H is finally obtained2S gas, which is essentially the coupling of two sets of absorption-desorption systems, obtains high-purity H through multiple absorption-desorption operations2And (4) S gas.
Patent CN 101054167A provides a high purity H2S separation process, 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, and finally the flash evaporated liquid phase enters a desorption tower to obtain high-purity H2S gas, which is improved in H by recycling regeneration gas and absorbing for multiple times2The purity of the S gas.
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.
Patent US 2008127831a1 provides a method for absorbing CO2Technique for gas post-multistage desorption, mainly taking into account downstream CO2The recovery device has higher operating pressure and adopts a one-step desorption mode, CO2The gas pressure is lower, which leads to the increase of the compression power consumption of the gas to a downstream device, thereby achieving the comprehensive optimization of the compression power consumption and the energy consumption of the desorption tower by configuring a plurality of stages of desorption towers with different pressures.
All current patents on acid gas purification devices are directed to downstream unitsA recovery device, which saves energy, reduces consumption or improves H2The gaseous purity' S of S technique, the utility model discloses based on the different demands of the required hydrogen sulfide purity of different sulphur chemicals, provide an acid gas purification technology and the device of producing multiple purity hydrogen sulfide, compare the technology of pursuit high-purity hydrogen sulfide of a taste, the utility model discloses regard as the process design direction with the product, have characteristics such as easy operation is nimble, with low costs and market strong adaptability.
SUMMERY OF THE UTILITY MODEL
The utility model relates to an acid gas purification process and 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), and the obtained H2The S gas generally enters a downstream sulfur device for recycling, the added value of the product is low, and the two most important factors in the whole acid gas purification device, namely the purity of the lean solvent and the impurity content 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.
The utility model discloses compare conventional technology to different sulphur chemicals are as the direction, utilize acid gas Component (CO)2、H2S, etc.) solubility differences in solvents-CO2Solubility lower than H2Solubility of S, preferential desorption of CO during desorption2Thus, by means of stepwise desorption, each H with increased purity is obtained in turn2And (4) S gas. Due to desorption pressure on CO2And H2The desorption rate of S is sensitive, so that in the design process, the parameters of the tower pressure and the like of each desorption tower can be adjusted and controlled to regulate and control each H2The purity of S gas meets the raw material purity requirements of different sulfur chemicals.
While obtaining more high-purity H2S gas, CO reduction in absorption process2I.e. increase of the solvent pair H2S selectivity, and thus the process design of the product-oriented acid gas purification plant, is more influenced by solvent selectivity than conventional designs, directly determining the yield of high-purity hydrogen sulfide in the processThe selection of parameters in the process design process can simultaneously consider two factors of energy consumption of the device and selectivity of the solvent.
In the design of the absorption column, due to H2S is absorbed faster than CO2The solvent selectivity can be improved by reducing the gas-liquid phase contact time in the column (e.g., reducing the column diameter). If the absorption tower is fed in multiple strands, a plurality of feed inlets are considered to be arranged, each feed position is optimized, and the gas phase quantity among the feed inlets is reduced compared with that when all streams enter from the bottom of the absorption tower, so that the tower diameter of the tower section among the feed inlets is reduced on the premise that equipment manufacturing is allowed, and the solvent selectivity is further improved by adopting a variable-diameter tower mode.
The technical scheme of the utility model:
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 which respectively desorb and suck hydrogen sulfide gas with different purities: h2S is more than or equal to 95 percent, high-purity hydrogen sulfide gas and H2The medium-purity hydrogen sulfide gas with S between 85 and 95 percent and H2S is low-purity hydrogen sulfide gas with the purity of 70-85%; comprehensively determining the number of desorption towers and the purity of hydrogen sulfide at the top of each desorption tower according to downstream requirements and device energy consumption, wherein the pressure of the desorption tower required for obtaining high-purity hydrogen sulfide gas is 0.05-0.1 MPa, the pressure of the desorption tower required for obtaining medium-purity hydrogen sulfide gas is 0.1-0.35 MPa, and the pressure of the desorption tower required for obtaining low-purity hydrogen sulfide gas is 0.35-0.8 MPa;
(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 step (2), the type of solvent used for absorption is selected from H2S solubility is better than CO2The solvent is one or More of Ethanolamine (MEA), Diethanolamine (DEA), Methyldiethanolamine (MDEA), and Diisopropanolamine (DIPA), preferably Methyldiethanolamine (MDEA).
The utility model has the advantages that: the utility model discloses based on the different demands of the required hydrogen sulfide purity of different sulphur chemicals, provide a produce the acid gas purification technology and the device of multiple purity hydrogen sulfide, compare the technology of pursuit high-purity hydrogen sulfide of a taste, the utility model discloses regard as the process design direction with the product, have characteristics such as easy operation is nimble, with low costs and market strong adaptability.
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 device of the utility model: 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 device 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 device 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 device 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 solution 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, which can be modified or wetted by one 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 utility model 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 original design adopts a conventional absorption-desorption process, and the two catalytic dry gases are mixed and enter the bottom of an absorption tower and are adopted by 40 percentwThe content of impurities is 0.06 percentwThe MDEA solution (subscript w is mass fraction, m is mole fraction, and the same applies later) ensures the purified gas at the top of the towerMiddle H2S content less than 20ppmvThe amount of the solvent is 35400kg/H, H is obtained at the top of the desorption tower2The purity of the S gas is 88.92%m(dry basis content, the same applies hereinafter), the petrochemical company has three sets of sulfur recovery devices, namely a NaHS device, a thiourea device and a sulfuric acid device, and the information of each product is shown in Table 2, so that H originally designed is obtained according to the purity of the raw material2And all S gas enters the thiourea device.
According to the design method of the utility model (the process flow is shown in figure 4), two catalytic dry gases enter different feed inlets according to the composition optimization, and the tower diameter of each section of the absorption tower is optimized according to the gas phase in the tower, the absorption tower adopts a reducing tower, and the lean solvent adopts 30 percentwThe impurity content is 0.04 percentwThe dosage of the lean solvent is 39150kg/h on the premise of ensuring the desulfurization effect of the MDEA solution, and 90.48 percent can be obtained by adopting a direct desorption modemH of (A) to (B)2S gas, visible solvent selectivity is improved, according to the comprehensive optimization of raw material requirements, economic benefits and the like of a downstream recovery device, a final desorption unit is matched with two desorption towers, the tower pressure of the first desorption tower is 0.17MPa (gauge pressure, the same applies later), and 85 percent is obtainedmH2The pressure of the second desorption tower is 0.05MPa, and 95 percent is obtainedmH2And (4) removing NaHS from S gas.
The detailed information of the two designs is shown in Table 3, and the original design is 58.58kmol/h 88.92%mH2The purity of S gas can only reach the raw material requirement of a thiourea device, and 24.82kmol/h 85.18 percent can be obtained by adopting a step-by-step desorption mode according to the design method of the utility modelmH2S gas is used as raw material of a thiourea device, and 32.67kmol/h 95.01%mH2The S gas is used as the raw material of the NaHS device, and compared with the original design, the added value of the product is greatly improved.
TABLE 1
TABLE 2
TABLE 3
Example 2:
on the basis of the example 1, the three-tower desorption process is adopted to respectively obtain the hydrogen sulfide with high, medium and low purity, and the tower pressure of the first desorption tower is 0.45MPa, the tower pressure of the second desorption tower is 0.18MPa, and the tower pressure of the third desorption tower is 0.05MPa as shown in figure 5. The detailed information of the two designs is shown in Table 4, the original design is 58.58kmol/h 88.92%mH2The purity of S gas can only reach the raw material requirement of a thiourea device, and 5.6kmol/h70.07 percent can be obtained by adopting a step-by-step desorption mode according to the design method of the utility modelmH2S gas is used as raw material of a sulfuric acid device, and the content of S gas is 15.7kmol/h 87.26%mH2S gas is used as a raw material of a thiourea device, and 36.19kmol/h is 95.22 percentmH2The S gas is used as the raw material of the NaHS device, the added value of the product is greatly improved compared with the original design, a small amount of low-purity hydrogen sulfide is obtained compared with the embodiment 1, and the yield of the high-purity hydrogen sulfide is improved.
TABLE 4
While the foregoing is directed to the preferred embodiment of the present invention, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the principles of the invention, and it is intended that such changes and modifications be considered as within the scope of the invention.
Claims (1)
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.
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| CN110548370A (en) * | 2019-09-04 | 2019-12-10 | 大连理工大学 | Acid gas purification process and device for producing hydrogen sulfide with various purities |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110548370A (en) * | 2019-09-04 | 2019-12-10 | 大连理工大学 | Acid gas purification process and device for producing hydrogen sulfide with various purities |
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