CN218231879U - Sulfur recovery system - Google Patents
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- CN218231879U CN218231879U CN202222403375.5U CN202222403375U CN218231879U CN 218231879 U CN218231879 U CN 218231879U CN 202222403375 U CN202222403375 U CN 202222403375U CN 218231879 U CN218231879 U CN 218231879U
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Abstract
The utility model provides a sulfur recovery system, including the acid gas combustion unit, sulphur recovery unit, the tail gas desulfurization unit that communicate in proper order, sulphur recovery unit includes integrated reactor, along flue gas flow direction, integrated reactor is including the one-level claus reaction section, second grade claus reaction section, hydrogenation reaction section, the oxidation reaction section that communicate in proper order, tail gas desulfurization unit includes tail gas heat exchanger, desulfurizing tower, the tail gas outlet of oxidation reaction section communicates with the high temperature medium runner inlet of tail gas heat exchanger, the tail gas inlet of desulfurizing tower communicates with the high temperature medium runner outlet of tail gas heat exchanger, the tail gas outlet of desulfurizing tower communicates with the low temperature medium runner of tail gas heat exchanger, set up the one-level desulfurization section, second grade desulfurization section, washing section, the defogging section that communicate in proper order in the desulfurizing tower; the utility model discloses can effectively improve sulphur rate of recovery, tail gas desulfurization efficiency, can reduce low sulfur recovery system's whole energy consumption level.
Description
Technical Field
The utility model relates to a sulphur recovery technical field, in particular to sulphur recovery system.
Background
For the modern chemical production, dry gas, low-component gas and circulating hydrogen generated in a hydrocracking device and a continuous reforming device are subjected to hydrogen sulfide removal by MDEA amine liquid, and then are regenerated into acid gas and acid water vapor containing hydrogen sulfide by a rich solvent, and if the acid gas containing hydrogen sulfide is directly discharged, the environment is polluted, the environmental protection is not facilitated, and a large amount of sulfur resources are wasted.
Therefore, in the prior art, sulfur recovery is often performed on the acid gas containing hydrogen sulfide by using sulfur recovery processes such as a direct oxidation method, an LO-cat process and the like. However, the existing sulfur recovery system is often high in energy consumption and relatively low in sulfur recovery rate, and brings a large load to tail gas desulfurization.
In addition, after carrying out sulphur and retrieving, still there can be certain high temperature tail gas among the sulphur recovery system, and prior art often just discharges tail gas through desulfurization treatment simply, not only causes thermal waste, is unfavorable for lowering system's whole energy consumption, is difficult to ensure moreover that tail gas fully desulfurizes, is unfavorable for the discharge to reach standard of tail gas.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at providing a sulfur recovery system to solve the energy consumption that the sulfur recovery system among the prior art exists and be on the high side, tail gas desulfurization efficiency lower scheduling problem.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this:
the utility model provides a sulfur recovery system, includes acid gas combustion unit, sulphur recovery unit, tail gas desulfurization unit that communicate in proper order, sulphur recovery unit includes the integration reactor, along flue gas flow direction, the integration reactor is including the one-level claus reaction section, second grade claus reaction section, hydrogenation reaction section, the oxidation reaction section that communicate in proper order, tail gas desulfurization unit includes tail gas heat exchanger, desulfurizing tower, the tail gas export of oxidation reaction section and the high temperature medium runner entry intercommunication of tail gas heat exchanger, the tail gas entry of desulfurizing tower and the high temperature medium runner export intercommunication of tail gas heat exchanger, the tail gas export of desulfurizing tower and the low temperature medium runner intercommunication of tail gas heat exchanger, set up the one-level desulfurization section, second grade desulfurization section, washing section, the defogging section that communicate in proper order in the desulfurizing tower.
Further, the sulphur recovery unit includes condenser unit, reheater subassembly, the condenser unit includes one-level sulphur cooler, second grade sulphur cooler, tertiary sulphur cooler, level four sulphur cooler, fifth sulphur condenser, the reheater subassembly includes one-level re-heater, second grade re-heater, tertiary re-heater, level four re-heater, along flue gas flow direction, set gradually one-level sulphur cooler, one-level re-heater between the flue gas outlet of acid gas combustion unit and the entry of one-level claus reaction section, set gradually second grade sulphur cooler, second grade re-heater between the export of one-level claus reaction section and the entry of second grade claus reaction section, set gradually tertiary sulphur cooler, tertiary re-heater between the export of second grade claus reaction section and the entry of hydrogenation reaction section, set gradually level four sulphur cooler, level four re-heater between the export of hydrogenation reaction section and the entry of oxidation reaction section, the export of oxidation reaction section sets up fifth sulphur condenser to high temperature medium runner entry through fifth sulphur condenser and tail gas heat exchanger communicates.
Furthermore, the sulfur recovery unit comprises a tail gas incineration assembly, a flue gas inlet of the tail gas incineration assembly is connected with a flue gas outlet of the fifth sulfur condenser, and a flue gas outlet of the tail gas incineration assembly is connected with a high-temperature medium flow passage inlet of the tail gas heat exchanger.
Further, along the flue gas flow direction, the tail gas incineration assembly comprises a tail gas catcher, a tail gas incinerator and a second steam generator which are sequentially communicated, a flue gas inlet of the tail gas catcher is connected with a flue gas outlet of the fifth sulfur condenser, and a flue gas outlet of the second steam generator is connected with a high-temperature medium flow passage inlet of the tail gas heat exchanger.
Further, the sulfur recovery system comprises a liquid sulfur collecting unit, wherein the liquid sulfur collecting unit is respectively connected with a liquid sulfur outlet of the primary sulfur cooler, a liquid sulfur outlet of the secondary sulfur cooler, a liquid sulfur outlet of the tertiary sulfur cooler, a liquid sulfur outlet of the four-stage sulfur cooler, a liquid sulfur outlet of the fifth sulfur condenser and a liquid sulfur outlet of the tail gas catcher. Further, the one-level desulfurization section is including the circulation pond at the bottom of the tower, one-level circulating pump, the one-level spray thrower that communicate in proper order, the second grade desulfurization section is including the first liquid collecting device, first liquid storage pot, second grade circulating pump, the second grade spray thrower that communicate in proper order, the washing section is including the second liquid collecting device, second liquid storage pot, tertiary circulating pump, the tertiary spray thrower that communicate in proper order.
Further, the primary desulfurization section is provided with a slurry cooler, and the slurry cooler is arranged at the outlet of the primary circulating pump.
Further, the desulfurizing tower comprises an oxidizing air pipeline, and the oxidizing air pipeline is respectively communicated with the tower bottom circulation tank and the first liquid storage tank.
Further, the secondary circulating pump is provided with a first branch pipe, an outlet of the secondary circulating pump is communicated with the tower bottom circulating pool through the first branch pipe, and the first branch pipe is provided with a first valve body; the three-level circulating pump is provided with a second branch pipe, an outlet of the three-level circulating pump is communicated with the first liquid storage tank through the second branch pipe, and the second branch pipe is provided with a second valve body.
Further, the acid gas combustion unit comprises an acid gas combustion furnace and a first steam generator which are connected in sequence.
Compared with the prior art, the sulfur recovery system of the utility model has the following advantages:
a sulphur recovery system, through setting up the integration reactor, carry out super U Claus sulphur and retrieve, not only can effectively improve the sulphur rate of recovery, improve four solitary reactors moreover and integrate into the integration reactor, can effectively reduce the occupation space of relevant equipment among the sulphur recovery system, be favorable to improving integrating, the orderliness of pipeline overall arrangement. In addition, the tail gas generated by sulfur recovery is subjected to two-stage desulfurization and one-stage water washing, so that the tail gas desulfurization efficiency can be effectively improved. Simultaneously, tail gas before the desulfurization and tail gas after the desulfurization carry out the heat transfer through the tail gas heat exchanger, the waste heat of tail gas before the desulfurization is utilized to heat tail gas after the desulfurization, on the one hand, make the exhaust gas temperature reach above the dew point, be favorable to eliminating white smoke, alleviate the corruption to advancing flue and chimney, improve the diffusivity of pollutant, on the other hand, reduce the sulphur that gets into the absorption tower and retrieve tail gas temperature, make the tail gas be in a relative low temperature state in getting into the desulfurizing tower, be favorable to guaranteeing desulfurization efficiency, simultaneously, also fully and rationally utilize tail gas waste heat to a certain extent, be favorable to reducing the whole energy consumption level of sulphur recovery system.
Drawings
The accompanying drawings, which form a part hereof, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without undue limitation. In the drawings:
FIG. 1 is a schematic view of a sulfur recovery apparatus for ULU Claus in a sulfur recovery system according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of a tail gas treatment system in a sulfur recovery system according to an embodiment of the present invention;
FIG. 3 is a schematic diagram of a circulation pipeline structure related to a first-stage desulfurization section, a second-stage desulfurization section and a water washing section of the desulfurization tower in FIG. 2 according to the embodiment of the present invention.
Description of reference numerals:
1. an integrated reactor; 2. a first-stage Claus reaction section; 3. a secondary Claus reaction section; 4. a hydrogenation reaction section; 5. an oxidation reaction section; 6. a tail gas heat exchanger; 7. a desulfurizing tower; 8. a first-stage desulfurization section; 9. a secondary desulfurization section; 10. a water washing section; 11. a demisting section; 12. an acid gas combustion furnace; 13. a first steam generator; 14. a primary sulfur cooler; 15. a secondary sulfur cooler; 16. a third-stage sulfur cooler; 17. a four-stage sulfur cooler; 18. a primary reheater; 19. a secondary reheater; 20. a third-stage reheater; 21. a fourth stage reheater; 22. a fifth sulfur condenser; 23. an exhaust gas trap; 24. a tail gas incinerator; 25. a second steam generator; 26. a liquid sulfur collection unit; 27. a tower bottom circulation tank; 28. a first-stage circulating pump; 29. a first stage sprayer; 30. a first liquid collection device; 31. a first liquid storage tank; 32. a second-stage circulating pump; 33. a secondary sprayer; 34. a second liquid collection device; 35. a second liquid storage tank; 36. a three-stage circulating pump; 37. a third stage sprayer; 38. a first branch pipe; 39. a first valve body; 40. a second branch pipe; 41. a second valve body; 42. a slurry cooler; 43. and oxidizing the air pipeline.
Detailed Description
The inventive concepts of the present disclosure will be described hereinafter using terms commonly employed by those skilled in the art to convey the substance of their work to others skilled in the art. These utility concepts may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein.
It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict. In the present application, "flue gas" and "tail gas" refer to gas streams containing elemental sulfur that require sulfur recovery (or desulfurization) so as not to be confused with gas streams such as steam, air, and hydrogen in the present application.
The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
In order to solve the problems of high energy consumption, relatively low sulfur recovery rate, low tail gas desulfurization efficiency and the like of a sulfur recovery system in the prior art, the present embodiment provides a sulfur recovery system, as shown in fig. 1-3, the sulfur recovery system includes an acid gas combustion unit, a sulfur recovery unit, and a tail gas desulfurization unit that are sequentially communicated, the sulfur recovery unit includes an integrated reactor 1, and along the flow direction of flue gas, the integrated reactor 1 includes a first-stage claus reaction section 2, a second-stage claus reaction section 3, a hydrogenation reaction section 4, and an oxidation reaction section 5 that are mutually independent and sequentially communicated, the tail gas desulfurization unit includes a tail gas heat exchanger 6 and a desulfurization tower 7, a tail gas outlet of the oxidation reaction section 5 is communicated with a high-temperature medium flow passage inlet of the tail gas heat exchanger 6, a tail gas inlet of the desulfurization tower 7 is communicated with a high-temperature medium flow passage outlet of the tail gas heat exchanger 6, a tail gas outlet of the desulfurization tower 7 is communicated with a low-temperature medium flow passage of the tail gas heat exchanger 6, and a first-stage desulfurization section 8, a second-stage desulfurization section 9, a water washing section 10, and a demisting section 11 that are sequentially communicated are arranged in the desulfurization tower 7.
The sulfur-containing gas generated by upstream equipment, such as regenerated acid gas, stripped acid gas and the like, enters an acid gas combustion unit for combustion, and the generated flue gas is subjected to two-stage Claus reaction, selective hydrogenation reaction and selective oxidation reaction in sequence for ultra-Youguos sulfur recovery. Wherein, flue gas A that produces behind super Yokous sulphur recovery enters desulfurizing tower 7 behind the heat transfer of tail gas heat exchanger 6, carries out two-stage desulfurization, washing, defogging, forms flue gas B, and B carries out the heat exchange back through tail gas heat exchanger 6 and A, satisfies the environmental protection and discharges the requirement and discharge.
Thereby this application is through setting up integrated reactor 1, carries out super you claus sulphur and retrieves, not only can effectively improve the sulphur rate of recovery, improves four solitary reactors moreover and integrates into integrated reactor 1, can effectively reduce the occupation space of relevant equipment among the sulphur recovery system, is favorable to improving integration, the orderliness of pipeline overall arrangement. In addition, the tail gas generated by sulfur recovery is subjected to two-stage desulfurization and one-stage water washing, so that the tail gas desulfurization efficiency can be effectively improved. Meanwhile, at the upper reaches of desulfurizing tower 7, low reaches, tail gas before the desulfurization and tail gas after the desulfurization carry out the heat transfer through tail gas heat exchanger 6, the waste heat of tail gas before the utilization desulfurization heats tail gas after the desulfurization, make the exhaust gas temperature reach above the dew point on the one hand, be favorable to eliminating white smoke, alleviate the corruption to advancing flue and chimney, improve the diffusivity of pollutant, on the other hand reduces the sulphur recovery tail gas temperature that gets into the absorption tower, make the tail gas be in a relative low temperature state in getting into desulfurizing tower 7, be favorable to guaranteeing desulfurization efficiency, and simultaneously, also fully and rationally utilize the tail gas waste heat to a certain extent, be favorable to reducing the whole energy consumption level of sulphur recovery system.
For ease of understanding, the sulfur recovery system is specifically described herein in terms of the flow of sulfur-containing gas.
The acid gas combustion unit comprises an acid gas combustion furnace 12 and a first steam generator 13 which are connected in sequence, wherein sulfur-containing gas generated by upstream equipment enters the acid gas combustion furnace 12 and is mixed with part of air to perform oxygen-deficient combustion to produce high-temperature flue gas. The main reactions in the acid gas burner 12 are: h 2 S+3/2O 2 →SO 2 +H 2 O，H 2 S+1/2SO 2 →H 2 O+3/4S 2 。
High temperature flue gas carries out the heat transfer through first steam generator 13, and the flue gas cools down to about 320 ℃ on the one hand to follow-up super you kelos sulphur recovery technology's going on, and the saturated steam of the first steam generator 13 by-product of on the other hand merges into the steam pipe network, uses for whole factory system, is favorable to reducing the whole energy consumption level of sulphur recovery system.
The sulfur recovery unit includes condenser unit, re-heater subassembly, and is specific, the condenser unit includes five condensers, is marked as one-level sulfur cooler 14, second grade sulfur cooler 15, tertiary sulfur cooler 16, level four sulfur cooler 17, fifth sulfur condenser 22 respectively, the re-heater unit includes four re-heaters, is marked as one-level re-heater 18, second grade re-heater 19, tertiary re-heater 20, level four re-heater 21 respectively.
Along the flow direction of the flue gas, a primary sulfur cooler 14 and a primary reheater 18 are sequentially arranged between the flue gas outlet of the first steam generator 13 and the inlet of the primary claus reaction section 2, so that the flue gas cooled to about 320 ℃ by the first steam generator 13 enters the primary sulfur cooler 14 to be cooled to about 160 ℃, liquid sulfur is separated, and meanwhile, byproduct steam is supplied to the whole plant area system for use, thereby being beneficial to reducing the overall energy consumption level of a sulfur recovery system; the flue gas then enters the primary reheater 18 and is heated to about 240 ℃. Preferably, the primary reheater 18 is heated electrically or by medium pressure superheated steam in a common system in the plant.
The heated flue gas enters a first-level Claus reaction section 2, and a conventional deoxidation protection type catalyst and a sulfur recovery (hydrolysis type) titanium-based catalyst are respectively filled in the first-level Claus reaction section 2, wherein the main chemical reaction is as follows: 2H 2 S+SO 2 →3/xS x +2H 2 O，COS+H 2 O→H 2 S+CO 2 ，CS 2 +2H 2 O→2H 2 S+CO 2 。
Along the flue gas flow direction, set up second grade sulfur cooler 15, second grade re-heater 19 between the export of one-level claus reaction section 2 and the entry of second grade claus reaction section 3 to the flue gas that one-level claus reaction section 2 came out gets into second grade sulfur cooler 15 and cools down to about 160 ℃, separates out liquid sulphur, and then the flue gas gets into second grade re-heater 19, is heated to about 220 ℃. Preferably, the secondary reheater 19 is heated by medium-pressure superheated steam in a plant-area utility system, which is beneficial to reducing the overall energy consumption level of the sulfur recovery system. Then, the flue gas enters a secondary Claus reaction section 3, and the secondary Claus reaction section 3 is filled with a conventional sulfur recovery titanium-based catalyst, wherein the main chemical reaction is：2H 2 S+SO 2 →3/xS x +2H 2 O。
Along the flue gas flow direction, set up tertiary sulfur cooler 16, tertiary re-heater 20 between the export of second grade claus reaction section 3 and the entry of hydrogenation section 4 to the flue gas that second grade claus reaction section 3 came out gets into tertiary sulfur cooler 16 and cools down to about 160 ℃, separates out liquid sulfur, and then the flue gas gets into tertiary re-heater 20, is heated to about 200 ℃. Preferably, the tertiary reheater 20 is heated by medium-pressure superheated steam in a plant-area common system, which is beneficial to reducing the overall energy consumption level of the sulfur recovery system. Then, the flue gas enters a hydrogenation reaction section 4, and a selective hydrogenation catalyst is filled in the hydrogenation reaction section 4, wherein the main chemical reaction is as follows: SO (SO) 2 +2H 2 →1/xS x +2H 2 O。
Along the flow direction of the flue gas, a four-stage sulfur cooler 17 and a four-stage reheater 21 are arranged between the outlet of the hydrogenation reaction section 4 and the inlet of the oxidation reaction section 5, so that the flue gas from the hydrogenation reaction section 4 enters the four-stage sulfur cooler 17 to be cooled to about 160 ℃, liquid sulfur is separated out, and then the flue gas and part of air are mixed and then enter the four-stage reheater 21 to be heated to about 205 ℃. Preferably, the four-stage reheater 21 is heated by medium-pressure superheated steam in a plant public system, which is beneficial to reducing the overall energy consumption level of the sulfur recovery system. Then, the flue gas enters an oxidation reaction section 5, and a selective oxidation catalyst is filled in the oxidation reaction section 5, wherein the main chemical reactions are as follows: 2H 2 S+O 2 →2/xS x +2H 2 O。
In the flow direction of the flue gas, the outlet of the oxidation reaction section 5 is provided with a fifth sulfur condenser 22 and is communicated with the high-temperature medium runner inlet of the tail gas heat exchanger 6 through the fifth sulfur condenser 22, so that the temperature of the flue gas discharged from the oxidation reaction section 5 is reduced to about 135 ℃ through the fifth sulfur condenser 22, liquid sulfur is separated, and meanwhile, the low-pressure saturated steam of 0.1MPaG is byproduct, and the deep condensation of the flue gas is realized.
The sulphur recovery unit includes that the tail gas burns the subassembly, the flue gas inlet that the subassembly was burned to the tail gas is connected with the flue gas outlet of fifth sulphur condenser 22, the flue gas outlet that the subassembly was burned to the tail gas is connected with the high temperature medium runner entry of tail gas heat exchanger 6 for carry out abundant burning to integrated reactor 1 exhaust tail gas, make the abundant reaction of sulfur-containing substance in the flue gas generate sulfur dioxide, so that follow-up tail gas desulfurization system's desulfurization operation.
Along the flow direction of the flue gas, the tail gas incineration assembly comprises a tail gas trap 23, a tail gas incinerator 24 and a second steam generator 25 which are sequentially communicated, the flue gas inlet of the tail gas trap 23 is connected with the flue gas outlet of the fifth sulfur condenser 22, and the flue gas outlet of the second steam generator 25 is connected with the high-temperature medium flow passage inlet of the tail gas heat exchanger 6. Wherein, flue gas through fifth sulphur condenser 22 by the deep condensation gets into tail gas trap 23 and carries out the sulphur separation, flue gas behind tail gas trap 23 gets into tail gas and burns burning furnace 24, and the flue gas that comes out from tail gas burning furnace 24 gets into second steam generator 25 and cools down to about 260 ℃ and then delivers to tail gas desulfurization system, and the by-product saturated steam merges in the steam pipe network simultaneously to supply whole factory system to use, be favorable to reducing sulphur recovery system's whole energy consumption level. The main reactions taking place in the tail gas incinerator 24 are: h 2 S+3/2O 2 →SO 2 +H 2 O，1/xS x +O 2 →SO 2 ，COS+3/2O 2 →SO 2 +CO 2 。
For the whole sulfur recovery unit, the ultra-Youkouse sulfur recovery process of 'two-stage Claus + selective hydrogenation + selective oxidation' is adopted, the total sulfur recovery rate reaches 99.5%, and the pollutant SO is reduced while the sulfur is produced in a large amount 2 The concentration entering the desulfurization unit has higher return on investment for long-period operation. In addition, for the condenser assembly, the first-stage sulfur cooler 14 and the second-stage sulfur cooler 15 share one shell pass, and the third-stage sulfur cooler 16 and the fourth-stage sulfur cooler 17 share one shell pass, so that a combined sulfur cooler structure is formed, on one hand, the number of devices and the occupied land area are reduced, on the other hand, the related pipeline layout is more concentrated and ordered, the control and regulation loop number on the cold side is favorably reduced, and the production operation is facilitated. At the same time, with conventional "ClausCompared with the sulfur recovery technology of reduction absorption, the sulfur recovery unit has the advantages of short process equipment, high integration degree, high system energy consumption utilization rate and simple and convenient production operation.
In the whole sulfur recovery unit, the first-stage sulfur cooler 14, the second-stage sulfur cooler 15, the third-stage sulfur cooler 16, the fourth-stage sulfur cooler 17, the fifth sulfur condenser 22 and the tail gas catcher 23 are used for condensing and separating liquid sulfur, the sulfur recovery system further comprises a liquid sulfur collection unit 26, and the liquid sulfur collection unit 26 is respectively connected with the liquid sulfur outlet of the first-stage sulfur cooler 14, the liquid sulfur outlet of the second-stage sulfur cooler 15, the liquid sulfur outlet of the third-stage sulfur cooler 16, the liquid sulfur outlet of the fourth-stage sulfur cooler 17, the liquid sulfur outlet of the fifth sulfur condenser 22 and the liquid sulfur outlet of the tail gas catcher 23, so that the liquid sulfur condensed and separated in the whole sulfur recovery unit is collected to facilitate subsequent sulfur processing.
For the tail gas desulfurization unit, an alkali washing desulfurization process is adopted, and the desulfurization solution is preferably a sodium hydroxide solution. The tail gas burns the subassembly and carries the flue gas A about 260 ℃ to tail gas desulfurization system, and flue gas A at first gets into tail gas heat exchanger 6, and after the heat transfer with the flue gas B after the desulfurizing tower 7 purifies, flue gas A temperature drop is about 180 ℃ and gets into the entry of desulfurizing tower 7, sets up the nozzle at desulfurizing tower 7 entrance, spouts the atomized water into flue gas A, makes flue gas A's moisture reach the saturation, and the temperature rapid cooling is to about 60 ℃ (saturation temperature) simultaneously. The temperature of the flue gas B reaches 110-120 ℃ after heat exchange, and the flue gas B is discharged through a chimney. The tail gas heat exchanger 6 is preferably a glass tube type heat exchanger, and on the basis of ensuring the heat exchange efficiency, the service life of the equipment can be fully ensured under the severe working condition of easy corrosion.
For the desulfurizing tower 7, the flue gas enters from the lower end of the desulfurizing tower 7 and goes through two independent desulfurizing sections, and the desulfurizing liquid is used for absorbing SO in the flue gas 2 And desulfurizing and purifying the flue gas. The flue gas after desulfurization and purification passes through a water washing section 10 and a demisting section 11 at the upper part of the desulfurizing tower 7 in sequence to remove redundant dust and fog drops.
For the first-stage desulfurization section 8, the desulfurization tower comprises a tower bottom circulating pool 27, a first-stage circulating pump 28 and a first-stage sprayer 29 which are sequentially communicated, wherein the tower bottom circulating pool 27 is used as a first-stage desulfurization circulating groove, the first-stage circulating pump 28 pumps the desulfurization liquid in the tower bottom circulating pool 27 to the first-stage sprayer 29, and the first-stage sprayer 29 sprays the desulfurization liquid, so that the desulfurization liquid is in countercurrent and contact with the flue gas in the first-stage desulfurization section 8, the first-stage desulfurization process is completed, and meanwhile, the desulfurization liquid falls into the tower bottom circulating pool 27 again to form the desulfurization circulation of the first-stage desulfurization section 8.
The secondary desulfurization section 9 comprises a first liquid collecting device 30, a first liquid storage tank 31, a secondary circulating pump 32 and a secondary sprayer 33 which are sequentially communicated. Wherein, the secondary desulfurization section 9 also adopts a desulfurization liquid circulation mode, which is basically consistent with the primary desulfurization section 8. What is different, the bottom of the secondary desulfurization section 9 is provided with a first liquid collecting device 30 for collecting the desulfurization liquid sprayed by the secondary sprayer 33, preferably, the first liquid collecting device 30 is a first liquid containing tower plate, the first liquid containing tower plate is arranged between the primary desulfurization section 8 and the secondary desulfurization section 9, the first liquid containing tower plate can be a bubble cap type tower plate, on one hand, flue gas passing through the primary desulfurization section 8 can enter the secondary desulfurization section 9 through the first liquid containing tower plate, on the other hand, the receiving and collecting of the desulfurization liquid in the secondary desulfurization section 9 can also be realized, then the desulfurization liquid in the secondary desulfurization section 9 flows into the first liquid storage tank 31, and is pumped to the secondary sprayer 33 by the secondary circulating pump 32 for cyclic spraying of the desulfurization liquid.
The water washing section 10 comprises a second liquid collecting device 34, a second liquid storage tank 35, a three-stage circulating pump 36 and a three-stage sprayer 37 which are sequentially communicated. The liquid circulating spray of each component in the water washing section 10 is consistent with the secondary desulfurization section 9, except that the secondary desulfurization section 9 is the circulation of the desulfurization liquid, and the water washing section 10 is the circulation of the process water. Meanwhile, the second liquid storage tank 35 is communicated with an external water source and is used for supplementing water to the washing circulation of the washing section 10.
In the first-stage desulfurization section 8, the second-stage desulfurization section 9 and the water washing section 10, the absorption liquid distributor and the packing layer are all matched, and the related distributor and the packing layer can adopt the prior art, which is not described herein again.
In addition, the three-stage circulating pump 36 has a second branch pipe 40, an outlet of the three-stage circulating pump 36 is communicated with the first liquid storage tank 31 through the second branch pipe 40, and the second branch pipe 40 is provided with a second valve body 41, so that part of circulating water in the water washing section 10 can be conveyed to the second-stage desulfurization section 9 according to actual needs, and water is supplemented to the desulfurization solution circulation of the second-stage desulfurization section 9. The second-stage circulating pump 32 is provided with a first branch pipe 38, the outlet of the second-stage circulating pump 32 is communicated with the tower bottom circulating pool 27 through the first branch pipe 38, and the first branch pipe 38 is provided with a first valve body 39, so that the desulfurization solution in the second-stage desulfurization section 9 can be conveyed to the first-stage desulfurization section 8 according to actual needs. The tower bottom circulation tank 27 is provided with a discharge port so as to discharge the desulfurization solution in the primary desulfurization section 8 according to actual needs.
For the demisting stage 11, which is disposed at the top of the desulfurization tower 7, a conventional wire demister is arranged. Preferably set up 2 layers of silk screen defogger, the tail gas that carries the mist rises with certain speed, and when the silk screen defogger through the frame on the grid for the inertia effect that the mist rises owing to the mist for the mist collides and the adhesion on the surface of filament with the filament, thereby realizes the defogging effect.
On the basis of the relevant structure of the desulfurizing tower 7, the tail gas discharged from the tail gas incinerator 24 has higher temperature and higher initial water content, so that the balance temperature of a desulfurizing unit is easily higher, the neutralization reaction of the sodium thiosulfate is not facilitated, and the desulfurizing efficiency is difficult to improve. Desulfurizing tower 7 includes slurry cooler 42, cools off the cooling through the desulfurization liquid in external cooling water or other cold sources and the desulfurizing tower 7, slurry cooler 42 can set up in the circulating line of one-level desulfurization section 8, also can set up in the circulating line of second grade desulfurization section 9. Preferably, the primary desulfurization section 8 is provided with a slurry cooler 42, and the circulating slurry in the primary desulfurization section 8 is cooled, so that the cooling and dehumidifying of the flue gas in the desulfurization tower 7 are indirectly completed, and the realization of higher desulfurization efficiency is guaranteed; the slurry cooler 42 may be located in the bottom circulation tank 27, either at the inlet of the primary circulation pump 28, or at the outlet of the primary circulation pump 28.
Considering that part of HSO is generated in the desulfurization process using the desulfurization solution 3 - 、SO 3 2- Ionic but actually SO is in desulfurization 4 2- The desired ions are obtained, and for this purpose, the desulfurization tower 7 includes an oxidizing air pipeline 43, and the oxidizing air pipeline 43 is respectively communicated with the tower bottom circulation tank 27 and the first liquid storage tank 31, and is used for introducing compressed air into the desulfurization solution in the tower bottom circulation tank 27 and the desulfurization slurry in the first liquid storage tank 31, so that oxygen in the air and HSO in the desulfurization solution are enabled to be 3 - 、SO 3 2- The ions are fully oxidized into sulfate ions through ion reaction, so that the sufficiency of desulfurization is ensured, and the desulfurization effect is favorably improved.
In whole tail gas desulfurization unit, through the relevant setting of "two-stage alkali wash circulation desulfurization + washing circulation + defogging" for tail gas desulfurization unit can the fully provided tail gas desulfurization demand among the sulphur recovery system, and can adapt to SO under the various operating modes 2 The concentration fluctuates, and continuous and stable standard emission is realized. Simultaneously, the tail gas desulfurization unit passes through slurry cooler 42, oxidation wind pipeline 43's setting, can adjust the temperature, the ionic composition of desulfurization thick liquid, is favorable to maintaining the desulfurization environment in whole desulfurizing tower 7 under a relative low temperature condition, ensures to reduce the temperature dehumidification of flue gas in desulfurizing tower 7 to improve desulfurization efficiency, also make the desulfurization thick liquid fully oxidize simultaneously, ensure abundant desulfurization, be favorable to improving desulfurization effect.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The utility model provides a sulfur recovery system, a serial communication port, sulfur recovery system is including the acid gas combustion unit, sulfur recovery unit, the tail gas desulfurization unit that communicate in proper order, sulfur recovery unit includes integrated reactor (1), along flue gas flow direction, integrated reactor (1) is including the one-level claus reaction section (2), second grade claus reaction section (3), hydrogenation reaction section (4), oxidation reaction section (5) that communicate in proper order, the tail gas desulfurization unit includes tail gas heat exchanger (6), desulfurizing tower (7), the export of oxidation reaction section (5) and the high temperature medium runner entry intercommunication of tail gas heat exchanger (6), the tail gas entry of desulfurizing tower (7) and the high temperature medium runner export intercommunication of tail gas heat exchanger (6), the tail gas export of desulfurizing tower (7) and the low temperature medium runner intercommunication of tail gas heat exchanger (6), set up the one-level desulfurization section (8), second grade desulfurization section (9), washing section (10), defogging section (11) that communicate in proper order in desulfurizing tower (7).
2. A sulfur recovery system according to claim 1, wherein said sulfur recovery unit comprises a condenser assembly, a reheater assembly, the condenser component comprises a primary sulfur cooler (14), a secondary sulfur cooler (15), a tertiary sulfur cooler (16), a quaternary sulfur cooler (17) and a fifth sulfur condenser (22), the reheater assembly comprises a primary reheater (18), a secondary reheater (19), a tertiary reheater (20) and a quaternary reheater (21), a primary sulfur cooler (14) and a primary reheater (18) are sequentially arranged between the flue gas outlet of the acid gas combustion unit and the inlet of the primary Claus reaction section (2) along the flow direction of flue gas, a secondary sulfur cooler (15) and a secondary reheater (19) are sequentially arranged between the outlet of the primary Claus reaction section (2) and the inlet of the secondary Claus reaction section (3), a tertiary sulfur cooler (16) and a tertiary reheater (20) are sequentially arranged between the outlet of the secondary Claus reaction section (3) and the inlet of the hydrogenation reaction section (4), a four-stage sulfur cooler (17) and a four-stage reheater (21) are sequentially arranged between the outlet of the hydrogenation reaction section (4) and the inlet of the oxidation reaction section (5), a fifth sulfur condenser (22) is arranged at the outlet of the oxidation reaction section (5), and is communicated with the high-temperature medium runner inlet of the tail gas heat exchanger (6) through a fifth sulfur condenser (22).
3. A sulfur recovery system according to claim 2, wherein the sulfur recovery unit comprises a tail gas incineration assembly, the flue gas inlet of which is connected with the flue gas outlet of the fifth sulfur condenser (22), and the flue gas outlet of which is connected with the high temperature medium flow channel inlet of the tail gas heat exchanger (6).
4. A sulfur recovery system according to claim 3, wherein along the flow direction of the flue gas, the tail gas burning component comprises a tail gas catcher (23), a tail gas burning furnace (24) and a second steam generator (25) which are communicated in sequence, the flue gas inlet of the tail gas catcher (23) is connected with the flue gas outlet of the fifth sulfur condenser (22), and the flue gas outlet of the second steam generator (25) is connected with the high-temperature medium flow passage inlet of the tail gas heat exchanger (6).
5. A sulfur recovery system according to claim 4 comprising a liquid sulfur collection unit (26), said liquid sulfur collection unit (26) being connected to the liquid sulfur outlet of the primary sulfur cooler (14), the liquid sulfur outlet of the secondary sulfur cooler (15), the liquid sulfur outlet of the tertiary sulfur cooler (16), the liquid sulfur outlet of the quaternary sulfur cooler (17), the liquid sulfur outlet of the fifth sulfur condenser (22), and the liquid sulfur outlet of the tail gas trap (23), respectively.
6. A sulfur recovery system according to claim 1, wherein said primary desulfurization section (8) comprises a tower bottom circulation tank (27), a primary circulation pump (28) and a primary sprayer (29) which are sequentially communicated, said secondary desulfurization section (9) comprises a first liquid collecting device (30), a first liquid storage tank (31), a secondary circulation pump (32) and a secondary sprayer (33) which are sequentially communicated, and said washing section (10) comprises a second liquid collecting device (34), a second liquid storage tank (35), a tertiary circulation pump (36) and a tertiary sprayer (37) which are sequentially communicated.
7. A sulfur recovery system according to claim 6, wherein said primary desulfurization section (8) is provided with a slurry cooler (42), said slurry cooler (42) being disposed at the outlet of the primary circulation pump (28).
8. A sulfur recovery system according to claim 6, wherein the desulfurization tower (7) comprises an oxidizing air pipe (43), and the oxidizing air pipe (43) is respectively communicated with the tower bottom circulation tank (27) and the first liquid storage tank (31).
9. A sulfur recovery system according to claim 6, wherein said secondary circulation pump (32) has a first branch pipe (38), the outlet of said secondary circulation pump (32) communicates with the bottom circulation tank (27) through the first branch pipe (38), said first branch pipe (38) is provided with a first valve body (39); the three-stage circulating pump (36) is provided with a second branch pipe (40), the outlet of the three-stage circulating pump (36) is communicated with the first liquid storage tank (31) through the second branch pipe (40), and the second branch pipe (40) is provided with a second valve body (41).
10. A sulfur recovery system according to claim 1, wherein said acid gas combustion unit comprises an acid gas combustion furnace (12) and a first steam generator (13) connected in series.
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| CN202222403375.5U CN218231879U (en) | 2022-09-09 | 2022-09-09 | Sulfur recovery system |
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