CN106621796B - Method and device for simultaneously removing carbonyl sulfide and carbon disulfide - Google Patents
Method and device for simultaneously removing carbonyl sulfide and carbon disulfide Download PDFInfo
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/80—Type of catalytic reaction
- B01D2255/808—Hydrolytic
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D2257/30—Sulfur compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/308—Carbonoxysulfide COS
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Abstract
The invention discloses a method and a device for simultaneously removing carbonyl sulfide and carbon disulfide, wherein a desulfurization device comprises a heat exchange system consisting of a cooling tower and a fixed bed reaction tower, a catalysis assisting system consisting of a stripping tower, a spray tower and a communicating pipe, a continuous operation system consisting of two fixed bed reaction towers, a catalyst regeneration system consisting of the heat exchange system and a regeneration spray system, and the like. The method has high desulfurization efficiency, the heat of high-temperature flue gas can be well utilized, the catalytic reaction efficiency is improved by recycling the product dilute sulfuric acid, the double reaction towers are respectively positioned in the catalytic reaction and catalyst regeneration stages, the continuous operation of the system can be ensured by the timing switching of the electromagnetic valve, and meanwhile, the elemental sulfur on the surface of the deactivated catalyst can be transferred into a liquid phase in the regeneration process, so that the extraction of the elemental sulfur in the subsequent process is facilitated.
Description
Technical Field
The invention relates to a method and a device for simultaneously removing carbonyl sulfide and carbon disulfide, belonging to the field of air pollution control.
Background
COS and CS as the main organic sulfur 2 Is widely used in industrial flue gas, such as yellow phosphorus tail gas, blast furnace tail gas, etc. The CS is discharged to the atmosphere in the industrial production and use process, and can cause serious pollution and harm to the environment and human body, and trace CS in the industrial production 2 And COS have toxic action on the catalyst, so that the catalytic effect and service life of the catalyst are seriously affected, CS 2 And COS also form H through a slow hydrolysis reaction 2 S, corroding production equipment, not only bringing great economic loss to industrial production, but also increasing equipment investment and product cost, and simultaneously COS and CS 2 Is also a waste of sulfur resources.
Catalytic hydrolysis method for removing COS and CS 2 The principle of (2) is as follows: COS and CS 2 With steam on a catalyst to convert to H 2 S, then H 2 S is removed in the subsequent working section, the reaction temperature of catalytic hydrolysis is generally lower than 200 ℃, the energy consumption is lower, side reactions are fewer, and most of raw material gas contains water vapor required by the hydrolysis process. At the same time, low temperature catalytic hydrolysis of COS and CS 2 The process can avoid side reactions such as raw gas pyrolysis, methanation and the like, so the method becomes the prior method for removing COS and CS 2 One of the hot spots in the research field.
Chinese patent CN 102886203a discloses the invention of a method for desulfurizing and demercurating flue gas. The invention sprays the water containing chlorine ions into the dry desulfurization, mercury removal and dust removal device of the circulating fluidized bed, and then purifies the flue gas. The method has higher desulfurization efficiency, but the removed sulfur-containing compound is SO 2 And no catalyst regeneration process. Chinese patent CN 103432861a discloses the invention of "sintering desulfurization white smoke removal system and its technological process". The invention purifies white smoke according to the sequence of desulfurization, water removal and temperature reduction. The method has higher desulfurization efficiency and lower energy consumption, but the sulfur-containing compound removed is SO 2 And no catalyst regeneration process. Chinese patent CN 103657368A discloses an invention of a method and apparatus for purifying flue gas by a dry method of desulfurizing, denitrating and removing mercury simultaneously. The invention adopts an adsorption mode to remove SO 2 NOx removal by reduction and Hg removal by oxidation. The method has higher desulfurization, denitrification and demercuration efficiency, but the removed sulfur-containing compound is SO 2 And no catalyst regeneration process. The method and the device for simultaneously removing carbonyl sulfide and carbon disulfide have high desulfurization efficiency, high automation degree, high integration level, continuous operation, high heat utilization rate and convenient sulfur recovery.
At present, no report is made on a method and a device for enhancing and simultaneously removing carbonyl sulfide and carbon disulfide by dilute sulfuric acid.
Disclosure of Invention
The invention aims to provide a method for simultaneously removing carbonyl sulfide and carbon disulfide, which has the advantages of high desulfurization efficiency, high automation degree, high integration level, continuous operation, high heat utilization rate and convenient sulfur recovery, and can effectively solve the problem of organic sulfur purification, and the method comprises the following specific steps:
(1) The high-temperature flue gas after the pre-dedusting treatment is cooled to 150-200 ℃ through a waste heat boiler, and then heat exchange is carried out through a cooling tower, so that the temperature of the flue gas is reduced to 60-100 ℃, and the temperature of cooling liquid is increased to 60-100 ℃.
(2) The cooled gas is carried into the fixed bed reaction tower through the action of the stripping tower, so that the dilute sulfuric acid in the stripping tower is carried into the fixed bed reaction tower.
(3) And (3) cooling liquid which absorbs heat and heats up in the step (1) flows into a heat exchange jacket of the fixed bed reaction tower, and the temperature of the catalyst in the reaction tower is increased to 60-100 ℃.
(4) The gas with dilute sulfuric acid is subjected to catalytic hydrolysis reaction (H is generated) in a fixed bed reaction tower 2 S、SO 2 Etc.).
(5) Generated SO 2 The gas enters the spray tower along with the air flow to generate sulfuric acid and sulfurous acid, the sulfuric acid and the sulfurous acid flow back to the stripping tower through the communicating pipe, and the purified gas is discharged from the outlet.
(6) The cooling liquid is discharged in the jacket of the fixed bed reaction tower and then enters the cooling tower again for recycling.
(7) The regenerated water flows into a fixed bed reaction tower to wash the deactivated catalyst, the sulfate and elemental sulfur on the surface of the catalyst are carried out to enter a sulfur recovery procedure, and the catalyst after washing is quickly dried under the heating action of a jacket to form the regenerated catalyst.
The molar concentration of dilute sulfuric acid in the stripping tower and the spraying tower is 0.01-0.1 mol/L.
The cooling liquid is a mixed liquid of ethanol and water, and the molar ratio of the ethanol to the water is 0.5-20:1.
The catalyst in the fixed bed reaction tower is a hydrolysis catalyst, for example: modified activated carbon catalysts, modified hydrotalcite-like catalysts, modified alumina catalysts, modified molecular sieve catalysts, modified metal oxide catalysts, and the like.
The invention further aims to provide a device for simultaneously removing carbonyl sulfide and carbon disulfide, which comprises a waste heat boiler 1, a cooling tower 2, a stripping tower 3, a fixed bed reaction tower I4, a fixed bed reaction tower II 5, a spray tower 6, a heat exchange pump I7, a heat exchange pump II 8, a regeneration pump 9, a spray pump 10, a communicating pipe 11, a stirrer 12 and a heat exchange jacket 13; the waste heat boiler 1 is communicated with the cooling tower 2, and the cooling tower 2 is communicated with the stripping tower 3; the stripping tower 3 is respectively communicated with a fixed bed reaction tower I4 and a fixed bed reaction tower II 5 through three-way electromagnetic valves; the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are communicated with the spray tower 6 through a three-way electromagnetic valve; the lower ends of the stripping tower 3 and the spray tower 6 are communicated through a communicating pipe 11, and the lower end of the spray tower 6 is communicated with the top end of the spray tower 6 through a spray pump 10; the inner walls of the cooling tower 2, the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are respectively provided with a heat exchange jacket 13; the regeneration water tank is communicated with the top ends of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 through a regeneration pump 9, and the bottoms of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are communicated with a sulfur recovery device; the outlet of the heat exchange pump II 8 is communicated with the top of the heat exchange jacket in the cooling tower 2, the bottom of the heat exchange jacket in the cooling tower 2 is respectively communicated with the tops of the heat exchange jackets in the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 through the heat exchange pump I7, and the bottoms of the heat exchange jackets in the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are communicated with the inlet of the heat exchange pump II 8 through a three-way electromagnetic valve.
The bottoms of the stripping tower 3 and the spraying tower 6 are respectively provided with a stirrer 12.
The invention discloses a method for preparing a catalyst by using a catalyst, which is characterized in that a regeneration flushing device is arranged in a fixed bed reaction tower I4 and a fixed bed reaction tower II 5, and a liquid storage tank is arranged at the bottom.
The principle of the invention is as follows: by using hydrolysis catalyst and by means of trace water vapor and O in flue gas 2 To make COS and CS 2 At the same time catalyze hydrolysis to H 2 S, byproduct SO generated under aerobic condition 2 Continuously oxidizing into sulfuric acid in the spraying process, and enabling the generated dilute sulfuric acid to enter a catalytic process along with air flow, so that desulfurization efficiency is enhanced, and the desulfurization reaction temperature is as follows: COS and CS at 60-100 DEG C 2 The removal efficiency is higher than 90%, and the main reactions are as follows:
the method has the advantages and technical effects that:
(1) The heat exchange system consisting of the cooling tower and the fixed bed reaction tower efficiently utilizes the temperature of the flue gas, and the catalyst can reach the proper reaction temperature without an additional heat source;
(2) The auxiliary catalytic system consisting of the stripping tower, the spray tower and the communicating pipe can be used for preparing by-product SO 2 The dilute sulfuric acid produced by recycling can play a role in enhancing the catalytic hydrolysis process;
(3) The catalyst regeneration system consisting of the heat exchange system and the regeneration spray system can utilize the heat provided by the heat exchange system to quickly dry the catalyst, so that the utilization efficiency of the heat is improved, and sulfur contained in waste liquid generated after regeneration can be reused;
(4) The stirrers at the bottoms of the spray tower and the stripping tower are used for adjusting the concentration balance of the dilute sulfuric acid in the liquid storage tank and between the liquid storage tanks.
(5) The continuous operation system composed of two fixed bed reaction towers can utilize the same set of heat exchange device and regeneration device to carry out the catalysis and regeneration process, and the characteristic of timing switching can be utilized, so that the reaction system can continuously work, and the degree of automation is high, and the integration level is high.
Drawings
FIG. 1 is a schematic view of the structure of the device according to the present invention;
FIG. 2 is a process flow diagram of the present invention.
In the figure: 1-a waste heat boiler; 2-a cooling tower; 3-stripping column; 4-a fixed bed reaction tower I; 5-a fixed bed reaction tower II; 6-a spray tower; 7-a heat exchange pump I; 8-a heat exchange pump II; 9-a regenerative pump; 10-a spray pump; 11-communicating pipe; 12-a stirrer; 13-heat exchange jacket.
Detailed Description
The present invention will be described in further detail with reference to specific examples, but the scope of the present invention is not limited to the following.
The device for the method for simultaneously removing carbonyl sulfide and carbon disulfide comprises a waste heat boiler 1, a cooling tower 2, a stripping tower 3, a fixed bed reaction tower I4, a fixed bed reaction tower II 5, a spray tower 6, a heat exchange pump I7, a heat exchange pump II 8, a regeneration pump 9, a spray pump 10, a communicating pipe 11, a stirrer 12 and a heat exchange jacket 13; the waste heat boiler 1 is communicated with the cooling tower 2, and the cooling tower 2 is communicated with the stripping tower 3; the stripping tower 3 is respectively communicated with a fixed bed reaction tower I4 and a fixed bed reaction tower II 5 through three-way electromagnetic valves; the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are communicated with the spray tower 6 through a three-way electromagnetic valve; the lower ends of the stripping tower 3 and the spray tower 6 are communicated through a communicating pipe 11, and the lower end of the spray tower 6 is communicated with the top end of the spray tower 6 through a spray pump 10; the inner walls of the cooling tower 2, the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are respectively provided with a heat exchange jacket 13; the regeneration water tank is communicated with the top ends of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 through a regeneration pump 9, and the bottoms of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are communicated with a sulfur recovery device; the outlet of the heat exchange pump II 8 is communicated with the top of the heat exchange jacket in the cooling tower 2, the bottom of the heat exchange jacket in the cooling tower 2 is respectively communicated with the tops of the heat exchange jackets in the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 through the heat exchange pump I7, and the bottoms of the heat exchange jackets in the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are communicated with the inlet of the heat exchange pump II 8 through a three-way electromagnetic valve; the bottoms of the stripping tower 3 and the spray tower 6 are provided with stirrers 12; the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are internally provided with regeneration flushing devices, and the bottoms of the regeneration flushing devices are provided with liquid storage tanks.
The cooling tower 2, the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 form a heat exchange system, the cooling tower 2 absorbs heat of flue gas and transfers the heat to cooling liquid, the warmed cooling liquid flows into the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 and releases heat, the catalyst is maintained at a proper reaction temperature, and the cooling liquid after releasing heat returns to the cooling tower 2 again to absorb heat, so that heat exchange circulation is performed.
The stripping tower 3, the spray tower 6 and the communicating pipe 11 are combined into a catalytic assisting system, and byproducts SO generated from the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 are formed 2 Dilute sulfuric acid is formed in the spray tower, and then flows back to the stripping tower 3 through the communicating pipe 11, and the dilute sulfuric acid in the stripping tower 3 is brought into the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 under the action of the stripping tower to enhance the catalytic hydrolysis, thereby achieving the auxiliary catalytic effect.
The heat exchange system and the regeneration spraying system form a regeneration system, the regeneration water enters a fixed bed reaction tower II 5 and a fixed bed reaction tower I4 which are positioned in the regeneration process stage, sulfate and sulfur on the surface of the catalyst are washed to a liquid storage tank at the bottom under the spraying action, the catalyst is dried under the heating of the heat exchange system, and waste liquid in the liquid storage tank is used for a subsequent sulfur extraction process.
The fixed bed reaction tower I4 and the fixed bed reaction tower II 5 form a continuous operation system, when one fixed bed reaction tower I4 is in a reaction process state, the other fixed bed reaction tower II 5 is in a regeneration process 5 state under the control of the electromagnetic valve, and the electromagnetic valve can automatically switch the working states of the two towers at regular intervals, so that the continuous operation function is achieved.
Example 1
The method for simultaneously removing carbonyl sulfide and carbon disulfide in the embodiment comprises the following steps:
(1) The high-temperature flue gas after the pre-dedusting treatment is cooled to 150 ℃ through the waste heat boiler 1, and then heat exchange is carried out through the cooling tower 2, so that the temperature of the flue gas is reduced to 60 ℃, and the temperature of the cooling liquid is increased to 60 ℃.
(2) The cooled gas is carried into a fixed bed reaction tower I4 and a fixed bed reaction tower II 5 by the action of a stripping tower 3, wherein the molar concentration of the dilute sulfuric acid in the stripping tower 3 is 0.01 mol/L.
(3) The cooling liquid with the temperature of 60 ℃ after absorbing heat and heating in the step (1) flows into heat exchange jackets of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5, and the temperature of the catalyst in the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 is increased to 60 ℃.
(4) The gas carrying dilute sulfuric acid undergoes catalytic hydrolysis reaction in a fixed bed reaction tower I4 and a fixed bed reaction tower II 5.
(5) Generated SO 2 The gas enters the spray tower 6 along with the air flow to generate sulfuric acid and sulfurous acid, the sulfuric acid and the sulfurous acid flow back to the stripping tower 3 through the communicating pipe 11, and the purified gas is discharged from the outlet.
(6) Cooling liquid releases heat in jackets of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 and then enters the cooling tower 2 again for recycling.
(7) The regenerated water flows into a fixed bed reaction tower I4 and a fixed bed reaction tower II 5 to flush the deactivated catalyst, sulfate and elemental sulfur on the surface of the catalyst are carried out to enter a sulfur recovery procedure, and the catalyst after water washing is quickly dried under the heating action of a jacket to form the regenerated catalyst.
The catalyst used in this example was an activated carbon catalyst Fe/AC modified with ferric nitrate.
By means of the method and the device, sulfur-containing flue gas (CS) 2 40ppm, 500ppm of COS, O 2 Concentration 1%, airspeed 80000h -1 ) Desulfurization experiments were performed with 100% CS 2 The removal rate and the removal rate of 100% of COS reach 600min and 540min respectively. This shows that the method and apparatus have good desulfurization effect.
Example 2
The method for simultaneously removing carbonyl sulfide and carbon disulfide in the embodiment comprises the following steps:
(1) The high-temperature flue gas after the pre-dedusting treatment is cooled to 200 ℃ through the waste heat boiler 1, and then heat exchange is carried out through the cooling tower 2, so that the temperature of the flue gas is reduced to 80 ℃, and the temperature of the cooling liquid is increased to 80 ℃.
(2) The cooled gas is carried into a fixed bed reaction tower I4 and a fixed bed reaction tower II 5 by the action of a stripping tower 3, wherein the molar concentration of dilute sulfuric acid in the stripping tower 3 is 0.06 mol/L.
(3) The coolant which absorbs heat and heats up in the step (1) flows into heat exchange jackets of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5, and the temperature of the catalyst in the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 is increased to 80 ℃.
(4) The gas carrying dilute sulfuric acid undergoes catalytic hydrolysis reaction in a fixed bed reaction tower I4 and a fixed bed reaction tower II 5.
(5) Generated SO 2 The gas enters the spray tower 6 along with the air flow to generate sulfuric acid and sulfurous acid, the sulfuric acid and the sulfurous acid flow back to the stripping tower 3 through the communicating pipe 11, and the purified gas is discharged from the outlet.
(6) Cooling liquid releases heat in jackets of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 and then enters the cooling tower 2 again for recycling.
(7) The regenerated water flows into a fixed bed reaction tower I4 and a fixed bed reaction tower II 5 to flush the deactivated catalyst, sulfate and elemental sulfur on the surface of the catalyst are carried out to enter a sulfur recovery procedure, and the catalyst after water washing is quickly dried under the heating action of a jacket to form the regenerated catalyst.
The catalyst used in this example is a hydrotalcite-like catalyst FeCuAlOx prepared from ferric nitrate, cupric nitrate, and aluminum nitrate.
By means of the method and the device, sulfur-containing flue gas (CS) 2 40ppm, 500ppm of COS, O 2 Concentration 1%, airspeed 80000h -1 ) Desulfurization experiments were performed with 100% CS 2 The removal rate and the removal rate of COS of 100% reach 840min and 630min respectively. This shows that the method and apparatus have good desulfurization effect.
Example 3
The method for simultaneously removing carbonyl sulfide and carbon disulfide in the embodiment comprises the following steps:
(1) The high-temperature flue gas after the pre-dedusting treatment is cooled to 180 ℃ through the waste heat boiler 1, and then heat exchange is carried out through the cooling tower 2, so that the temperature of the flue gas is reduced to 95 ℃, and the temperature of the cooling liquid is increased to 95 ℃.
(2) The cooled gas is carried into a fixed bed reaction tower I4 and a fixed bed reaction tower II 5 by the action of a stripping tower 3, wherein the molar concentration of the dilute sulfuric acid in the stripping tower 3 is 0.1mol/L.
(3) The cooling liquid with the temperature of 95 ℃ after absorbing heat and heating in the step (1) flows into heat exchange jackets of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5, and the temperature of the catalyst in the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 is increased to 95 ℃.
(4) The gas carrying dilute sulfuric acid undergoes catalytic hydrolysis reaction in a fixed bed reaction tower I4 and a fixed bed reaction tower II 5.
(5) Generated SO 2 The gas enters the spray tower 6 along with the air flow to generate sulfuric acid and sulfurous acid, the sulfuric acid and the sulfurous acid flow back to the stripping tower 3 through the communicating pipe 11, and the purified gas is discharged from the outlet.
(6) Cooling liquid releases heat in jackets of the fixed bed reaction tower I4 and the fixed bed reaction tower II 5 and then enters the cooling tower 2 again for recycling.
(7) The regenerated water flows into a fixed bed reaction tower I4 and a fixed bed reaction tower II 5 to flush the deactivated catalyst, sulfate and elemental sulfur on the surface of the catalyst are carried out to enter a sulfur recovery procedure, and the catalyst after water washing is quickly dried under the heating action of a jacket to form the regenerated catalyst.
The catalyst used in this example is an activated alumina catalyst Fe/Al modified with copper nitrate 2 O 3 。
By means of the method and the device, sulfur-containing flue gas (CS) 2 40ppm, 500ppm of COS, O 2 Concentration 1%, airspeed 80000h -1 ) Desulfurization experiments were performed with 100% CS 2 The removal rate and the removal rate of COS of 100% reach 720min and 570min respectively. This shows that the method and apparatus have good desulfurization effect.
Claims (5)
1. A method for simultaneously removing carbonyl sulfide and carbon disulfide is characterized by comprising the following specific steps:
(1) The high-temperature flue gas subjected to the pre-dedusting treatment is cooled to 150-200 ℃ through a waste heat boiler, then heat exchange is carried out through a cooling tower, the temperature of the flue gas is reduced to 60-100 ℃, and the temperature of cooling liquid is increased to 60-100 ℃;
(2) The cooled gas is carried into a fixed bed reaction tower through the action of a stripping tower, so that dilute sulfuric acid in the stripping tower is carried into the fixed bed reaction tower;
(3) The coolant which absorbs heat and heats up in the step (1) flows into a heat exchange jacket of a fixed bed reaction tower, and the temperature of a catalyst in the reaction tower is increased to 60-100 ℃;
(4) The gas carrying dilute sulfuric acid undergoes catalytic hydrolysis reaction in a fixed bed reaction tower;
(5) Generated SO 2 The gas enters a spray tower along with the air flow to generate sulfuric acid and sulfurous acid, the sulfuric acid and the sulfurous acid flow back to a stripping tower through a communicating pipe, and purified gas is discharged from an outlet;
(6) Cooling liquid releases heat in a jacket of the fixed bed reaction tower and then enters the cooling tower again for recycling;
(7) The regenerated water flows into a fixed bed reaction tower to wash the deactivated catalyst, the sulfate and elemental sulfur on the surface of the catalyst are carried out to enter a sulfur recovery procedure, and the catalyst after washing is quickly dried under the heating action of a jacket to form the regenerated catalyst.
2. The method for simultaneously removing carbonyl sulfide and carbon disulfide according to claim 1, wherein the method comprises the following steps: the molar concentration of the dilute sulfuric acid in the stripping tower and the spraying tower is 0.01-0.1 mol/L.
3. The method for simultaneously removing carbonyl sulfide and carbon disulfide according to claim 1, wherein the method comprises the following steps: the cooling liquid is a mixed liquid of ethanol and water, and the molar ratio of the ethanol to the water is 0.5-20:1.
4. The method for simultaneously removing carbonyl sulfide and carbon disulfide as claimed in claim 1, wherein: the catalyst in the fixed bed reaction tower is a hydrolysis catalyst.
5. The utility model provides a device of simultaneous removal carbonyl sulfide, carbon disulfide which characterized in that: the device comprises a waste heat boiler (1), a cooling tower (2), a stripping tower (3), a fixed bed reaction tower I (4), a fixed bed reaction tower II (5), a spray tower (6), a heat exchange pump I (7), a heat exchange pump II (8), a regeneration pump (9), a spray pump (10), a communicating pipe (11), a stirrer (12) and a heat exchange jacket (13); the waste heat boiler (1) is communicated with the cooling tower (2), and the cooling tower (2) is communicated with the stripping tower (3); the stripping tower (3) is respectively communicated with the fixed bed reaction tower I (4) and the fixed bed reaction tower II (5) through three-way electromagnetic valves; the fixed bed reaction tower I (4) and the fixed bed reaction tower II (5) are communicated with the spray tower (6) through a three-way electromagnetic valve; the lower ends of the stripping tower (3) and the spray tower (6) are communicated through a communicating pipe (11), and the lower end of the spray tower (6) is communicated with the top end of the spray tower (6) through a spray pump (10); the inner walls of the cooling tower (2), the fixed bed reaction tower I (4) and the fixed bed reaction tower II (5) are respectively provided with a heat exchange jacket (13); the regeneration water tank is communicated with the top ends of the fixed bed reaction tower I (4) and the fixed bed reaction tower II (5) through a regeneration pump (9), and the bottoms of the fixed bed reaction tower I (4) and the fixed bed reaction tower II (5) are communicated with a sulfur recovery device; the outlet of the heat exchange pump II (8) is communicated with the top of the heat exchange jacket in the cooling tower (2), the bottom of the heat exchange jacket in the cooling tower (2) is respectively communicated with the tops of the heat exchange jackets in the fixed bed reaction tower I (4) and the fixed bed reaction tower II (5) through the heat exchange pump I (7), and the bottoms of the heat exchange jackets in the fixed bed reaction tower I (4) and the fixed bed reaction tower II (5) are communicated with the inlet of the heat exchange pump II (8) through a three-way electromagnetic valve;
the bottoms of the stripping tower (3) and the spraying tower (6) are provided with stirrers (12);
the inside of the fixed bed reaction tower I (4) and the fixed bed reaction tower II (5) is provided with a regeneration flushing device, and the bottom is provided with a liquid storage tank.
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