A controllable heat-transfer sulfur recovery system

Abstract

This application relates to a controllable heat transfer sulfur recovery system, which includes a reaction unit and a sulfur increase unit. The reaction unit includes a controllable heat transfer reaction device and a connecting pipeline. The controllable heat transfer reaction device includes a catalytic oxidation reactor and a steam drum. The interior of the catalytic oxidation reactor includes multi-ring corrugated cooling pipes. The top and bottom ends of the corrugated cooling pipes are respectively aggregated into a steam outlet main pipe and a water inlet main pipe. The water inlet main pipe is connected to the steam drum through an external upper water delivery pipeline. A water delivery flow regulating valve is respectively arranged on the upper water delivery pipeline. A boiler water flow regulating valve is arranged on the boiler water delivery pipeline connected to the steam drum. In the present invention, the sulfur components in the acid gas can be recovered to the maximum extent, and no residue is generated in the tail gas, thereby ensuring the up-to-standard discharge of the tail gas. At the same time, through the controllable heat transfer recovery system, energy recovery is realized and by-product steam is produced.

Description

Technical Field

[0001] This application relates to a desulfurization and purification device for acid gas in the production processes of coal chemical industry, natural gas projects, etc. Specifically, it relates to a controllable heat transfer sulfur recovery system. Background Art

[0002] Common sulfur recovery processes include molten sulfur recovery, conventional Claus, sub-dew point Claus, selective catalytic oxidation sulfur recovery process, etc.

[0003] Molten sulfur recovery: It uses liquid phase to absorb H2S, and then reacts with O2 in the air to generate elemental sulfur. These sulfur are separated through flotation in a jet regeneration tank to form sulfur foam. The sulfur foam flows into a molten sulfur kettle through an intermediate tank. In the molten sulfur kettle, external steam heating is used to make the sulfur in a molten state, and then water is separated to recover sulfur paste. The main disadvantage of this method is low sulfur recovery efficiency (below 90%). Using this method to recover sulfur from acid gas in large chemical production plants cannot meet environmental protection requirements.

[0004] Conventional Claus reaction technology: Distinguished from the corresponding low-temperature Claus reaction, it refers to the Claus reaction carried out under conditions higher than the sulfur dew point temperature, and a sulfur separation device is set behind the reactor. Due to the high reaction temperature, the reaction equilibrium is not conducive to moving towards the direction of sulfur generation. Therefore, compared with the low-temperature Claus technology, its sulfur recovery rate is below 98%.

[0005] Low-temperature Claus technology: It refers to the Claus reaction carried out under conditions lower than the sulfur dew point temperature. The characteristics of this type of tail gas treatment method are that 2 - 3 low-temperature converters are configured behind the sulfur recovery device, and the reaction temperature is about 130°C. Due to the low reaction temperature, the reaction equilibrium moves significantly towards the direction of sulfur generation, and part of the liquid sulfur generated is immediately deposited on the catalyst. Therefore, the converter needs to be regenerated periodically and switched for use, and its sulfur recovery rate can reach over 99%.

[0006] Selective catalytic oxidation sulfur recovery process: When the H2S content in the acid gas is lower than 15% (V), the conventional split-flow Claus method is no longer applicable. And for lean acid gas or tail gas with an H2S content lower than 5% (V), it is even more difficult to treat. For example: in the associated gas of oil fields and the desulfurization of coal-derived syngas, the H2S content in the MDEA desulfurized regenerated gas is 2 - 5%, and its sulfur recovery cannot be fully recovered, and the tail gas needs to rely on incineration for further desulfurization. Similarly, for the NHD desulfurized regenerated gas in the desulfurization of coal-derived syngas with an H2S content of 2 - 5%, the same problem exists.

[0007] In order to overcome the situation that when the H2S content in acid gas is lower than 15% (V), the molten sulfur sulfur recovery technology, Claus technology, and conventional catalytic oxidation sulfur recovery no longer meet the current environmental protection emission requirements. Therefore, it is necessary to seek and develop a sulfur recovery process for dealing with acid gas with an H2S content lower than 15% (V), and this process should fully meet the environmental protection emission requirements, while recovering energy and reducing energy consumption. Summary of the Invention

[0008] The purpose of this application is to provide a controllable heat transfer sulfur recovery system. By providing a catalytic oxidation reactor, it is applicable to acid gas with an H2S concentration of 1% - 15%. By setting up an increased sulfur recovery system, the desulfurization accuracy and sulfur recovery rate are improved, ensuring that the tail gas meets the emission standards. At the same time, through the controllable heat transfer system, energy is recovered and by-product steam is produced.

[0009] To achieve the above purpose, the present invention provides a controllable heat transfer sulfur recovery system, including a reaction unit and a sulfur increased recovery unit. The reaction unit includes a first acid gas preheater, a hydrolysis reactor, a second acid gas preheater, a third acid gas preheater, a controllable heat transfer reaction device, and connecting pipelines;

[0010] The sulfur increased recovery unit includes a medium-temperature condenser, a sulfur separator, a low-temperature condenser, an adsorption reaction device, a tail gas detector, and connecting pipelines;

[0011] The controllable heat transfer reaction device includes a catalytic oxidation reactor and a steam drum. The catalytic oxidation reactor includes an upper reaction zone;

[0012] The upper reaction zone is filled with a catalyst. Vertically passing through the catalyst are multiple corrugated cooling tubes. The multiple corrugated cooling tubes are arranged annularly around the axis of the reactor, forming multiple rings of corrugated cooling tubes from the inside to the outside along the radial direction of the reactor. The number of the corrugated cooling tubes is determined according to the acid gas volume and composition;

[0013] The tops of the corrugated cooling tubes are aggregated to an annular steam outlet main pipe located at the top of the upper reaction zone, and the bottoms of the corrugated cooling tubes are aggregated to an annular water inlet main pipe located at the bottom of the upper reaction zone;

[0014] The water inlet main pipe is partitioned and blocked by a plugging block, and the steam outlet main pipe is partitioned and blocked by a plugging block. The corrugated cooling tubes corresponding to each partition are grouped;

[0015] Corresponding to the partitioned water inlet main pipe, there are water inlet short pipe interfaces connected. The water inlet short pipe interfaces are respectively connected to the steam drum through external upper water delivery pipelines, and water delivery flow regulating valves are respectively arranged on the upper water delivery pipelines;

[0016] Steam outlet headers with partition settings are correspondingly connected with steam outlet short pipe interfaces, and the steam outlet short pipe interfaces are respectively connected with a steam drum through an externally connected upper steam transmission pipeline;

[0017] The setting positions of the plugging blocks on the water inlet main pipe and the steam outlet main pipe correspond to each other vertically;

[0018] The steam drum is connected with a boiler water transmission pipeline, and a boiler water flow regulating valve is arranged on the boiler water transmission pipeline.

[0019] In an optional embodiment, the water inlet flow of the upper water transmission pipeline is regulated by the water transmission flow regulating valve, and the water inlet flow is controlled according to the outlet temperature of the catalytic oxidation reactor.

[0020] In an optional embodiment, the water inlet main pipe includes multiple water inlet branch pipes arranged in a ring and communicating with each other, including an inner ring water inlet branch pipe, a middle ring water inlet branch pipe, and an outer ring water inlet branch pipe;

[0021] The plugging blocks are respectively arranged on the water inlet branch pipes to conduct partition blocking on different water inlet branch pipes;

[0022] The water inlet branch pipes in each partition are communicated through a water inlet connecting pipe, and the water inlet connecting pipe is arranged in the same radial direction of the water inlet branch pipes;

[0023] The water inlet connecting pipe includes an inner side water inlet connecting pipe arranged between the inner ring water inlet branch pipe and the middle ring water inlet branch pipe, and an outer side water inlet connecting pipe arranged between the outer ring water inlet branch pipe and the middle ring water inlet branch pipe;

[0024] The inner side water inlet connecting pipe and the outer side water inlet connecting pipe are communicated with the steam outlet short pipe interface through the partition-blocked water inlet branch pipes.

[0025] In an optional embodiment, the steam outlet main pipe includes multiple steam outlet branch pipes arranged in a ring and communicating with each other, including an inner ring steam outlet branch pipe, a middle ring steam outlet branch pipe, and an outer ring steam outlet branch pipe;

[0026] The plugging blocks are respectively arranged on the steam outlet branch pipes to conduct partition blocking on different steam outlet branch pipes;

[0027] The steam outlet branch pipes in each partition are communicated through a steam outlet connecting pipe, and the steam outlet connecting pipe is arranged in the same radial direction of the steam outlet branch pipes;

[0028] The steam outlet connecting pipe includes an inner steam outlet connecting pipe disposed between the inner ring steam outlet branch pipe and the middle ring steam outlet branch pipe, and an outer steam outlet connecting pipe disposed between the outer ring steam outlet branch pipe and the middle ring steam outlet branch pipe;

[0029] The inner steam outlet connecting pipe and the outer steam outlet connecting pipe communicate with the steam outlet short pipe interface through the steam outlet branch pipes with partition barriers.

[0030] In an alternative embodiment, the catalytic oxidation reactor further includes a lower reaction zone filled with a catalyst. Multiple straight pipe cooling pipes vertically penetrate through the catalyst, and the multiple straight pipe cooling pipes are arranged in a ring around the axis of the reactor. The number of the straight pipe cooling pipes is determined according to the acid gas volume and composition, and both ends thereof are respectively connected to a steam header located at the top of the lower reaction zone and a boiler water header located at the bottom of the lower reaction zone. The steam header is connected to a lower steam outlet main pipe, the pipe orifice of the lower steam outlet main pipe extends out of the reactor and is connected to the steam drum through a lower steam transmission pipeline, and the boiler water header is connected to a lower water inlet main pipe, and the lower water inlet main pipe extends out of the reactor and is connected to the steam drum through a lower water transmission pipeline;

[0031] The set number and pipe size of the corrugated cooling pipes and the straight pipe cooling pipes respectively correspond to the reaction rate and heat release amount of the upper reaction zone and the lower reaction zone.

[0032] In an alternative embodiment, the cold side of the first acid gas preheater, the hydrolysis reactor, the cold side of the second acid gas preheater, the cold side of the third acid gas preheater, the catalytic oxidation reactor, the hot side of the second acid gas preheater, and the hot side of the first acid gas preheater are sequentially connected through pipelines;

[0033] The hydrolysis reactor is connected with a steam supplement pipeline, an air supplement pipeline is connected between the hydrolysis reactor and the cold side of the second acid gas preheater, and the cold side of the first acid gas preheater is connected with an intake pipeline.

[0034] In an alternative embodiment, the hot side of the first acid gas preheater, the hot side of the medium-temperature condenser, the sulfur separator, the hot side of the low-temperature condenser, the adsorption reaction device, and the tail gas detector are sequentially connected through pipelines;

[0035] The cold side of the medium-temperature condenser is connected with a medium-temperature boiler water pipeline and the produced steam is introduced into the steam outlet main pipe connected to the steam drum through a medium-temperature steam pipeline;

[0036] The adsorption reaction device is connected to the intake pipeline of the catalytic oxidation reactor through a purge gas pipeline, a purge gas induced draft fan, and a purge gas supply pipeline connected in sequence.

[0037] In an alternative embodiment, the adsorption reaction device includes a first adsorption reactor and a second adsorption reactor arranged in parallel, and three groups of inlet pipeline valve sets and two groups of outlet pipeline valve sets are arranged in parallel between the first adsorption reactor and the second adsorption reactor;

[0038] Each group of pipeline valve sets includes a common ventilation main pipe, two branch control valves, and ventilation branch pipes respectively connected to the first adsorption reactor and the second adsorption reactor.

[0039] In an alternative embodiment, the outlet pipeline valve sets include a first outlet pipeline valve set and a second outlet pipeline valve set;

[0040] The first outlet pipeline valve set is used to output clean gas. The tail gas detector is connected to the clean gas discharge pipeline connected to the ventilation main pipe of the first outlet pipeline valve set, and a clean gas extraction pipeline is connected to the clean gas discharge pipeline upstream of the tail gas detector. The clean gas extraction pipeline is connected to a clean gas extraction fan, and the clean gas extraction fan is connected to the ventilation main pipe of one group of inlet pipeline valve sets through a clean gas supply pipeline;

[0041] The second outlet pipeline valve set is used to internally circulate and export purge gas, and the root of the purge gas pipeline is connected to the ventilation main pipe of the second outlet pipeline valve set;

[0042] The inlet pipeline valve sets include a first inlet pipeline valve set, a second inlet pipeline valve set, and a third inlet pipeline valve set. The first inlet pipeline valve set is used to introduce regenerated acid gas, and the ventilation main pipe is connected to the cold side of the third acid gas preheater through a pipeline;

[0043] The second inlet pipeline valve set is used to introduce the tail gas after sulfur separation, and the ventilation main pipe is connected to the hot side of the low-temperature condenser through a pipeline;

[0044] The third inlet pipeline valve set is used to introduce clean gas for purging, and the clean gas supply pipeline is connected to the ventilation main pipe of the third inlet pipeline valve set.

[0045] In an alternative embodiment, both the first adsorption reactor and the second adsorption reactor internally include an upper adsorption zone and a lower reaction zone, and there is a gap between the upper adsorption zone and the lower reaction zone;

[0046] The upper adsorption zone is filled with adsorbent, and the lower reaction zone is filled with Claus catalyst. Both the adsorbent and the Claus catalyst are supported by inert ceramic balls.

[0047] Through the controllable heat transfer sulfur recovery system in this application, it is possible to effectively treat low-concentration H2S sour gas with an H2S content lower than 15% (V). By controlling the temperature of the reaction zone in the catalytic oxidation reactor in the form of controllable heat transfer, it can adapt to the treatment requirements of sour gas with different H2S concentrations, achieving the purpose of controllable heat transfer.

[0048] At the same time, for the controllable heat transfer in the reaction zone, it can adapt to the treatment of sour gas with different throughputs, reducing the impact of fluctuations in the amount of sour gas discharged from the upstream device on the desulfurization treatment effect.

[0049] In addition, the present invention can control the temperature of the reaction area, and can specifically adjust the working conditions of the catalyst in a specific reaction area, ensuring the overall long-term balance during the operation of the reaction zone and extending the service life of the catalytic oxidation catalyst.

[0050] The sulfur recovery system can achieve the synergistic recovery of sulfur, improve the desulfurization accuracy of sour gas and the sulfur recovery rate, and ensure the up-to-standard discharge of tail gas.

[0051] At the same time, the sulfur recovery system in the present invention can maximize the recovery of sulfur components in sour gas and ensure that no residue is generated in the tail gas, thereby ensuring the up-to-standard discharge of tail gas.

[0052] By performing controllable heat transfer on the core reaction area of the catalytic oxidation reactor, it is possible to recover the heat release and cooling forms during the catalytic oxidation reaction process, realize energy recovery, and by-product steam.

[0053] Other features and advantages of this application will be described in detail in the subsequent specific implementation section. Brief Description of the Drawings

[0054] In order to more clearly illustrate the technical solutions of the embodiments of this application, the following will briefly introduce the drawings required for the embodiments. It should be understood that the following drawings only show some embodiments of this application, and therefore should not be regarded as limiting the scope. For those of ordinary skill in the art, without creative efforts, other relevant drawings can also be obtained based on these drawings.

[0055] Figure 1 It is a schematic structural diagram of the controllable heat transfer sulfur recovery system in this application;

[0056] Figure 2 It is a schematic structural diagram of the catalytic oxidation reactor;

[0057] Figure 3 It is a schematic layout structural diagram of one form of partition of the corrugated cooling tube in the upper reaction zone;

[0058] Figure 4Schematic diagram of the layout structure of another form of zoning of the corrugated cooling pipe in the upper reaction zone;

[0059] Figure 5 Schematic diagram of the layout structure of the straight pipe cooling pipe in the lower reaction zone;

[0060] Figure 6 Schematic diagram of the structure of the corrugated cooling pipe;

[0061] Figure 7 Schematic diagram of the structure of the adsorption reactor.

[0062] Icon:

[0063] 1 - First acid gas preheater;

[0064] 2 - Hydrolysis reactor; 21 - Steam make-up pipeline; 22 - Air make-up pipeline; 23 - Inlet pipeline;

[0065] 3 - Second acid gas preheater; 4 - Third acid gas preheater;

[0066] 5 - Catalytic oxidation reactor; 5a - Upper reaction zone; 5b - Lower reaction zone; 5c - Catalyst;

[0067] 51 - Corrugated cooling pipe; 511 - Inner ring corrugated cooling pipe; 512 - Middle ring corrugated cooling pipe; 513 - Outer ring corrugated cooling pipe;

[0068] 500 - Plugging block;

[0069] 501 - Inner ring water inlet branch pipe; 502 - Middle ring water inlet branch pipe; 503 - Outer ring water inlet branch pipe; 504 - First upper water delivery pipeline; 505 - Second upper water delivery pipeline; 506 - First water inlet short pipe interface; 507 - Second water inlet short pipe interface;

[0070] 521 - Inner ring steam outlet branch pipe; 522 - Middle ring steam outlet branch pipe; 523 - Outer ring steam outlet branch pipe; 524 - First upper steam delivery pipeline; 525 - Second upper steam delivery pipeline; 526 - First steam outlet short pipe interface; 527 - Second steam outlet short pipe interface;

[0071] 52 - Boiler water delivery pipeline; 52a - First water delivery flow regulating valve; 52b - Second water delivery flow regulating valve; 52c - Boiler water flow regulating valve;

[0072] 53 - Straight pipe cooling pipe; 54 - Steam header; 55 - Boiler water header; 56 - Lower steam outlet main pipe; 57 - Lower steam delivery pipeline; 58 - Lower water inlet main pipe; 59 - Lower water delivery pipeline;

[0073] 6 - Medium-temperature condenser; 61 - Medium-temperature boiler water pipeline; 62 - Medium-temperature steam pipeline;

[0074] 7 - Sulfur separator; 8 - Low - temperature condenser;

[0075] 9 - Adsorption reaction device; 9a - First adsorption reactor; 9b - Second adsorption reactor; 9c - Adsorbent; 9d - Claus catalyst; 91 - First gas outlet pipeline valve group; 92 - Second gas outlet pipeline valve group; 93 - First gas inlet pipeline valve group; 94 - Second gas inlet pipeline valve group; 95 - Third gas inlet pipeline valve group; 10 - Tail gas detector; 11 - Steam drum; 12 - Purge gas pipeline; 13 - Purge gas induced draft fan; 14 - Purge gas supply pipeline; 15 - Clean gas discharge pipeline; 16 - Clean gas induced gas pipeline; 17 - Clean gas induced draft fan; 18 - Clean gas supply pipeline;

[0076] V1 - First control valve; V2 - Second control valve; V3 - Third control valve; V4 - Fourth control valve; V5 - Fifth control valve; V6 - Sixth control valve; V7 - Seventh control valve; V8 - Eighth control valve; V9 - Ninth control valve; V10 - Tenth control valve. Detailed implementation manners

[0077] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions in the embodiments of this application will be clearly and completely described below in conjunction with the accompanying drawings in the embodiments of this application. Obviously, the described embodiments are part of the embodiments of this application, rather than all of them. Usually, the components of the embodiments of this application described and illustrated in the accompanying drawings here can be arranged and designed in various different configurations.

[0078] In the description of this application, it should be noted that the orientation or positional relationship indicated by terms such as "inside", "outside", etc. is based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship in which the product of this application is usually placed when in use. It is only for the convenience of describing this application and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this application. In addition, terms such as "first", "second", etc. are only used for descriptive distinction and cannot be understood as indicating or implying relative importance.

[0079] In the description of this application, it should also be noted that unless otherwise clearly specified and limited, the terms "set", "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be directly connected, or indirectly connected through an intermediate medium, and it can be the communication inside two elements. For those of ordinary skill in the art, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0080] The controllable heat transfer sulfur recovery system in this application is mainly applied to the desulfurization treatment of low-concentration H2S acid gas with H2S content less than 15% (V) in acid gas and sulfur recovery. Specifically, by changing the structure of the reaction device and setting up a sulfur increase system, the controllable heat transfer of the catalytic oxidation reactor and sulfur increase are realized, ensuring that acid gas with different H2S concentrations of 1% - 15% by volume can be desulfurized, improving the desulfurization accuracy and sulfur recovery rate, and ensuring that the tail gas meets the emission standards.

[0081] The most important aspects of the controllable heat transfer reaction device and sulfur recovery system are the two key technical points of controllable heat transfer and sulfur increase. At the same time, through the mutual cooperation of the reaction unit and the sulfur increase unit, a synergistic cross-correlation is formed between desulfurization treatment and sulfur increase, and ultimately, relatively high desulfurization accuracy and sulfur recovery rate are ensured.

[0082] See Figure 1 and in combination with Figure 2 as well as Figure 7 Before elaborating on the technical solutions in this application, a brief description of the desulfurization and sulfur recovery system in this application is given from the overall process level.

[0083] The low-concentration H2S acid gas transported from upstream is first heated by the waste heat of the downstream reaction tail gas, and after heating up, it enters the hydrolysis reactor 2 and reacts with a small amount of steam to obtain hydrolysis, so that organic sulfur such as COS and CS2 in the acid gas is hydrolyzed into H2S that is easy to remove.

[0084] After hydrolysis, the acid gas is mixed with an appropriate amount of air and continues to be heated by the waste heat of the downstream reaction tail gas. After heating up, part of it undergoes a catalytic oxidation reaction, and the other part is used for the regeneration of the downstream adsorption reactor.

[0085] The catalytic oxidation reaction of the acid gas is specifically carried out inside the catalytic oxidation reactor 5. The catalytic oxidation reaction is carried out through the catalyst 5c bed filled with the catalytic oxidation catalyst 5c inside the catalytic oxidation reactor 5. At the same time, there are two reaction zones, upper and lower, inside the catalytic oxidation reactor 5, and cooling temperature control and heat transfer are carried out through the cooling tube groups in the two reaction zones.

[0086] Under the action of the catalyst 5c, H2S is directly oxidized to elemental sulfur by O2. By adjusting the reaction conditions, the reaction temperature of the catalyst 5c bed can be controlled at ≤300°C, and at the same time, the acid gas tail gas contains a small amount of SO2 and no H2S. The catalytic oxidation reaction is an exothermic reaction in the reactor. The bed layer is cooled by the boiler water introduced into the cooling tube group, and at the same time, the steam generated during the cooling process is aggregated to the steam drum 11 for use by other devices.

[0087] The tail gas of the reaction gas after catalytic oxidation treatment passes through multiple preheaters in sequence to preheat the acid gas. After most of the reaction heat is released, it is cooled by a condenser for sulfur separation and recovery, and then the tail gas of the reaction is adsorbed to remove SO2 in the tail gas after low-temperature condensation, and finally meets the discharge standards.

[0088] At the same time, the adsorbent 9c saturated with SO2 adsorption is desorbed by the regenerated gas containing H2S obtained after upstream hydrolysis, and after undergoing a regeneration reaction through the Claus catalyst 9d, the inner circulation of the regenerator containing elemental sulfur generated during the regeneration process is returned to sulfur recovery.

[0089] From the perspective of acid gas catalytic oxidation, combined with Figures 1 - 6 , one of the core technical points in the present invention is to provide a controllable heat transfer reaction device, including a catalytic oxidation reactor 5 and a steam drum 11, and the catalytic oxidation reactor 5 includes an upper reaction zone 5a.

[0090] Since the acid gas enters from the top of the catalytic oxidation reactor 5, the main catalytic oxidation reaction also takes place in the upper reaction zone 5a. That is to say, the upper reaction zone 5a belongs to the main reaction area. This application is mainly used to control the reaction temperature in the upper reaction zone 5a for controllable heat transfer.

[0091] The upper reaction zone 5a is filled with catalytic oxidation catalyst 5c, and the catalyst 5c is supported by inert porcelain balls. The filled catalytic oxidation catalyst 5c constitutes the catalyst 5c bed layer of the upper reaction zone 5a. Under the action of the catalyst 5c, most of the H2S in the acid gas is directly oxidized by O2 into elemental sulfur. The mixed gas removing most of the H2S enters the lower reaction zone 5b, and the remaining H2S is directly oxidized by O2 into elemental sulfur. Heat exchange tubes are arranged in the catalyst 5c bed layers of both the upper reaction zone 5a and the lower reaction zone 5b. By introducing boiler water into the heat exchange tubes to cool the bed layer temperature, the bed layer temperature is controlled ≤ 300 °C. The reactions occurring are:

[0092]

[0093]

[0094] From the perspective of controllable heat transfer in the main reaction area of the upper reaction zone 5a, multiple corrugated cooling tubes 51 are vertically connected through the catalyst 5c. The multiple corrugated cooling tubes 51 constitute the cooling tubes of the upper reaction zone 5a. Further, the multiple corrugated cooling tubes 51 are arranged in a ring along the axial direction of the reactor, forming multiple-ring corrugated cooling tubes 51 arranged from the inside to the outside along the radial direction of the reactor. The number of corrugated cooling tubes 51 is determined according to the acid gas volume and composition.

[0095] Specifically, the top ends of each ring of corrugated cooling pipes 51 are respectively aggregated to a steam outlet main pipe arranged in a ring shape at the top of the upper reaction zone 5a, and the bottom ends of each ring of corrugated cooling pipes 51 are respectively aggregated to a water inlet main pipe arranged in a ring shape at the bottom of the upper reaction zone 5a.

[0096] That is to say, each ring of corrugated cooling pipes 51 is correspondingly provided with a steam outlet main pipe and a water inlet main pipe arranged in a ring shape on both the top and bottom sides, and both the steam outlet main pipe and the water inlet main pipe are connected to the steam drum 11 through pipelines.

[0097] During the cooling process, the boiler water transported from the steam drum 11 enters each corrugated cooling pipe 51 through the water inlet main pipe at the bottom. The boiler water flows from bottom to top and uses the latent heat of vaporization to cool the reaction bed layer during the flow process. At the same time, its phase transformation converts into steam and is aggregated to the steam outlet main pipe at the top, and then the steam returns to the steam drum 11.

[0098] Combined with the attached drawings, the corrugated cooling pipes 51 in the present application include an inner ring corrugated cooling pipe 511, a middle ring corrugated cooling pipe 512, and an outer ring corrugated cooling pipe 513, and the catalytic oxidation catalyst 5c is filled between the multi-ring corrugated cooling pipes 51.

[0099] Through the multi-ring arrangement form of the corrugated cooling pipes 51, the cooling pipes of different ring groups can correspond to different parts in the radial direction of the main reaction area, maintaining full coverage of the reaction area.

[0100] In the present application, the specific number of rings and the quantity of the corrugated cooling pipes 51 are not limited. The set quantity and pipeline size of the corrugated cooling pipes 51 in the upper reaction zone 5a correspond to the reaction rate and heat release amount in the upper reaction zone 5a. Specifically, the set quantity and pipeline size of the corrugated cooling pipes 51 in the upper reaction zone 5a can be adjusted according to the flow rate of the pickling gas and the type and model of the filled catalytic oxidation catalyst 5c under different working conditions to meet the cooling requirements of the upper reaction zone 5a.

[0101] Based on the adjustment of the reaction temperature, it is mainly carried out by controlling the feed water volume of the boiler water in the water inlet main pipe.

[0102] At the same time, in order to achieve controllable heat transfer of the reaction temperature in different reaction areas of different upper reaction zones 5a, by partitioning the water inlet main pipe and the steam outlet main pipe, different corrugated cooling pipes 51 are grouped in different zones in the upper reaction zone 5a.

[0103] Specifically, the main water inlet pipe is partitioned and blocked by the blocking block 500. The corrugated cooling pipes 51 corresponding to each partition are set in groups. The main water inlet pipe with partitioned settings is correspondingly connected with water inlet short pipe interfaces. The water inlet short pipe interfaces are respectively connected with the steam drum 11 through the externally connected upper water conveying pipelines, and water conveying flow regulating valves are respectively arranged on each upper water conveying pipeline, so as to realize the regulation of the water supply amount of the boiler water flow in the corrugated cooling pipes 51 in groups in each partition.

[0104] Furthermore, each pipe section of the main water inlet pipe in each partition corresponds to an upper water conveying pipeline, and the water conveying flow regulating valves on each upper water conveying pipeline are independently controlled, which can keep the overall flow rate of the boiler water supply stable, and can increase or decrease the water supply amount of the boiler water supply simultaneously.

[0105] Specifically, the water inlet flow rate of the upper water conveying pipeline is regulated by the water conveying flow regulating valve, and the water inlet flow rate is controlled according to the outlet temperature of the catalytic oxidation reactor 5. To elaborate, a temperature sensor is arranged on the outlet pipeline of the catalytic oxidation reactor 5. The temperature sensor and the water conveying flow regulating valve are respectively electrically connected to the control system to establish a temperature-flow control loop, and the water inlet flow rate of the boiler water is controlled and regulated according to the gas temperature at the outlet of the catalytic oxidation reactor 5.

[0106] From the perspective of control regulation, it can be to keep the same flow rate of the boiler water in the upper water conveying pipelines corresponding to each pipe section of the main water inlet pipe in each partition, and the flow rate of the boiler water in each upper water conveying pipeline can be adjusted to increase or decrease synchronously. This working condition corresponds to the up and down fluctuations of the acidic gas volume entering the upper reaction zone 5a.

[0107] At the same time, it can also keep different flow rates of the boiler water in the upper water conveying pipelines corresponding to each pipe section of the main water inlet pipe in each partition, and the flow rate of the boiler water in each upper water conveying pipeline can be independently adjusted to increase or decrease. This working condition corresponds to the controllable heat transfer adjustment of different reaction zones of the bed layer.

[0108] Specifically, combined with Figure 3 In it, the main water inlet pipe is divided into left and right partitions by the blocking block 500, and the multi-ring distributed corrugated cooling pipes 51 are set in the form of left and right groups, constituting the water inlet form of the upper water conveying pipeline to the left and right sides in the catalytic oxidation reactor 5, so as to control and regulate the reaction conditions of the catalyst 5c in different parts of the reactor specifically. Thus, the adjustment of the catalyst 5c in the above different regions can be carried out. The adjustment of the use of the catalyst 5c can be understood as the targeted switching protection of the operating conditions of the catalyst 5c.

[0109] For example, when most of the sour gas enters the reactor through the gap between the top steam outlet headers, the flow rate of the boiler water in the upper water supply pipeline on the left side can be increased to significantly cool the catalyst 5c bed layer on the left side. At the same time, the minimum flow rate that can prevent the corrugated cooling pipe 51 on the right side of the reactor from being damaged by heat is controlled and maintained in the upper water supply pipeline on the right side. That is to say, the minimum flow rate is correspondingly set according to the pipe diameter and length of the corrugated cooling pipe 51, which can comprehensively consider the most severe working conditions of the corrugated cooling pipe 51 and minimize the impact of heat damage to the corrugated cooling pipe 51.

[0110] Combined with the heat transfer in the overall reaction bed layer, on the premise that the bed layer temperature is controlled ≤ 300 °C to meet the catalytic oxidation reaction in which H2S in different reaction zones can be directly oxidized by O2 into elemental sulfur, on the one hand, the catalyst 5c bed layer on the left side can be protected to be fully cooled and maintained under relatively mild reaction conditions, and on the other hand, the protection of the corrugated cooling pipe 51 can be taken into account, and the catalyst 5c bed layer on the right side can be allowed to fully carry out the exothermic reaction. Thus, the technical purpose of specifically controlling the reaction conditions in different reaction zones on the left and right sides can be achieved.

[0111] When most of the sour gas enters the reactor through the gap between the top steam outlet headers, the flow rate of the boiler water in the upper water supply pipeline on the right side can be increased to significantly cool the catalyst 5c bed layer on the right side. At the same time, the minimum flow rate that can prevent the corrugated cooling pipe 51 on the left side of the reactor from being damaged by heat is controlled and maintained in the upper water supply pipeline on the left side. Combined with the heat transfer in the overall reaction bed layer, on the premise that the bed layer temperature is controlled ≤ 300 °C to meet the catalytic oxidation reaction in which H2S in different reaction zones can be directly oxidized by O2 into elemental sulfur, on the one hand, the catalyst 5c bed layer on the right side can be protected to be fully cooled and maintained under relatively mild reaction conditions, and on the other hand, the protection of the corrugated cooling pipe 51 can be taken into account, and the catalyst 5c bed layer on the left side can be allowed to fully carry out the exothermic reaction. Thus, the technical purpose of specifically controlling the reaction conditions in different reaction zones on the left and right sides can be achieved.

[0112] By installing a water flow regulating valve on the independent upper water supply pipeline corresponding to the corrugated cooling pipe 51 after zoning into groups, the above-mentioned sub-region control can be achieved. Further, the control and adjustment of the reaction conditions in different reaction zones can be realized, the technical effect of controllable heat transfer and controlling the temperature of the reaction zone can be achieved, and at the same time, the overall coordination and balance of the operation of the catalyst 5c inside the reactor can be realized, and the long-term service life of the catalyst 5c can be extended.

[0113] Furthermore, by using two independently controlled water flow regulating valves, when the acid gas concentration is high, the two water flow regulating valves can be simultaneously opened at a large opening to maintain a high water inlet flow rate to achieve temperature control; when the acid gas concentration is low, one of the water flow regulating valves is kept at a minimum flow rate, and the bed temperature is adjusted by opening the other water flow regulating valve normally, thereby protecting the catalyst 5c around the corrugated cooling pipe 51 corresponding to the normal opening, and extending the service life of the entire catalyst 5c, and vice versa.

[0114] The corrugated cooling tube 51 in the present invention is mainly in the form of a thin-walled carbon steel tube, which can fully exchange heat and ensure good heat exchange efficiency. The relatively thin wall thickness of 1-2 mm enables the boiler water introduced into the corrugated cooling tube 51 to fully absorb the temperature released by the reaction bed and utilize the latent heat of evaporation of the boiler water. At the same time, combined with the maintenance of the minimum flow rate mentioned above, the corrugated cooling tube 51 can be kept stable and reliable under the condition of efficient cooling and heat exchange.

[0115] Under the premise of the above-mentioned water inlet regulation and control of the reaction temperature conditions, in order to realize the external transmission of by-product steam by the corrugated cooling pipes 51 after being divided into groups, the steam outlet main pipe is partitioned and blocked by the blocking blocks 500, and the corrugated cooling pipes 51 corresponding to each partition are arranged in groups. The corrugated cooling pipes 51 formed by the blocking blocks 500 on the water inlet main pipe are partitioned and grouped. In order to realize normal water inlet and steam outlet, the setting position of the blocking blocks 500 on the water inlet main pipe corresponds to the setting position of the blocking blocks 500 on the steam outlet main pipe. That is to say, based on the overlap of the upper and lower corresponding projections of the water inlet main pipe and the steam outlet main pipe, the upper and lower corresponding blocking blocks 500 on the water inlet main pipe and the steam outlet main pipe can separate the multi-ring corrugated cooling pipes 51 into multiple groups of independent water inlet and steam outlet pipe groups. Combined with the set water supply flow regulating valve, the water supply amount of different pipe groups can be adjusted, and the normal external transmission of by-product steam can be realized.

[0116] The steam outlet main pipes arranged in different zones are connected to corresponding steam outlet short pipe interfaces, which are connected to the steam drum 11 through external upper steam transmission pipelines. Figure 3 In the structure, the steam outlet main pipe is divided into left and right partitions by a blocking block 500, and the corrugated cooling pipes 51 in the corresponding area are separated and set into two groups of the same form. The steam outlet main pipe corresponding to the corrugated cooling pipes 51 is connected to the steam drum 11 through two external upper steam pipelines. Specifically, the steam converted by the phase change of boiler water in each group of corrugated cooling pipes 51 is merged into the upper steam pipeline and introduced into the steam drum 11 through the corresponding independent steam outlet main pipe partition section, which can reduce the mutual interference of the corrugated cooling pipes 51 in different groups.

[0117] It should be noted that the steam drum 11 in this application is a pressurized device. The steam pressure generated in the steam drum 11 provides the conveying pressure for the boiler feed water. At the same time, the by-product steam pressure in the cooling pipes in the reactor is greater than the pressure in the steam drum 11. Therefore, the flow of water conveyance and steam conveyance can be maintained relatively.

[0118] At the same time, the steam drum 11 is connected to a boiler water conveying pipeline 52, which is mainly used to introduce boiler water into the steam drum 11 and enable the boiler water to enter the cooling pipes in the reactor through the water conveying pipeline. From the perspective of controllable heat transfer, it also lies in controlling and adjusting the boiler water flow regulating valve 52c provided on the boiler water conveying pipeline 52.

[0119] Specifically, during the reaction process, the external makeup water of the boiler water and the external delivery of steam are continuous dynamic processes. The boiler water flow regulating valve 52c can control the dynamic makeup water flow of the steam drum 11, and then control the amount of externally produced steam of the steam drum 11 from the perspective of adjusting the liquid level of the steam drum 11. Therefore, from this perspective, the flow regulation of the boiler water can also indirectly play a role in regulating the temperature of the reaction zone, and then combine with the flow rate of the boiler water introduced into the cooling pipes to achieve the technical purpose of overall controllable heat transfer and controlling the temperature of the upper reaction zone 5a.

[0120] More specifically, since the treatment amount of the acid gas fluctuates and cannot be actually controlled, the heat release amount and temperature in the upper reaction zone 5a cannot be accurately predicted. In order to control the reaction temperature in the upper reaction zone 5a and timely remove the reaction heat, the amount of boiler water introduced into the upper reaction zone 5a by the steam drum 11 through the water flow regulating valve cannot be accurately maintained at a relatively stable flow rate. However, in order to ensure that the reaction temperature is controlled within a reasonable range, it is necessary to ensure that the supply amount of the boiler water introduced into the upper reaction zone 5a by the water flow regulating valve can achieve the basic purpose of controllable heat transfer. That is to say, no matter how dynamically the supply amount changes, there is a most concerned basis, which is to follow the reaction rate of the catalytic oxidation catalyst 5c with the fluctuation or uncertainty of the acid gas flow rate and maintain the controllability of the reaction temperature in the upper reaction zone 5a.

[0121] This process results in a dynamic change in the amount of boiler water passed from the steam drum 11 to the upper reaction zone 5a, which is reflected in the change in the by-product steam, i.e., the amount of steam input to the steam drum 11. Since the by-product steam is directly discharged in real time, when the amount of boiler water passed from the steam drum 11 to the upper reaction zone 5a increases, and the steam input from the reactor to the steam drum 11 and the amount of by-product steam discharged increase, the boiler water level in the steam drum 11 decreases. Therefore, water is replenished by opening the boiler water flow regulating valve 52c, or the opening of the boiler water flow regulating valve 52c is increased during the water replenishment process, so that the liquid level of the steam drum 11 is maintained in a relatively stable range, so that the dynamic changes of different factors are aggregated to the angle of maintaining the stable liquid level of the steam drum 11, thereby achieving the ultimate substantial purpose of controllable heat transfer.

[0122] A liquid level meter (not shown in the figure) is provided inside the steam drum 11 in the present invention. By electrically connecting the boiler water flow regulating valve 52c and the liquid level meter, and electrically connecting the liquid level meter and the boiler water flow regulating valve 52c and the control module, the opening of the boiler water flow regulating valve 52c is adjusted at the PLC automatic control angle.

[0123] In one specific embodiment, see Figure 3 In the partitioning form, based on the partitioning and blocking of the two sides of the water inlet main pipe by the blocking block 500, in order to keep the boiler water feed water entering the reactor from the upper water pipes located on both sides and to be supplied to the corrugated cooling tubes 51 grouped in different partitions, the water inlet main pipe includes a plurality of water inlet branch pipes arranged in a ring and interconnected, including an inner ring water inlet branch pipe 501, a middle ring water inlet branch pipe 502 and an outer ring water inlet branch pipe 503.

[0124] The blocking blocks 500 are respectively arranged on the water inlet branch pipes to isolate different water inlet branch pipes. That is to say, two blocking blocks 500 are arranged on the inner ring water inlet branch pipe 501, the middle ring water inlet branch pipe 502 and the outer ring water inlet branch pipe 503, which separate the inner ring water inlet branch pipe 501, the middle ring water inlet branch pipe 502 and the outer ring water inlet branch pipe 503 into two relatively independent pipe sections. In order to enable the water inlet branch pipes at different positions to supply water to the corresponding corrugated cooling pipes 51, the water inlet branch pipes of each partition are connected through the water inlet connecting pipe, and the water inlet connecting pipe The pipe is arranged in the same radial direction of the water inlet branch pipe, so that the water inlet branch pipes after partition blocking can be connected. Furthermore, the water inlet connecting pipe includes an inner water inlet connecting pipe arranged between the inner ring water inlet branch pipe 501 and the middle ring water inlet branch pipe 502, and an outer water inlet connecting pipe arranged between the outer ring water inlet branch pipe 503 and the middle ring water inlet branch pipe 502, so as to realize the communication of the pipe cavities of the inner ring water inlet branch pipe 501, the middle ring water inlet branch pipe 502 and the outer ring water inlet branch pipe 503.

[0125] The inner water inlet connecting pipe and the outer water inlet connecting pipe are communicated with the water inlet short pipe interface through the water inlet branch pipes with partition barriers.

[0126] The inner ring water inlet branch pipe 501 corresponding to the inner ring corrugated cooling pipe 511 is communicated with the middle ring water inlet branch pipe 502 corresponding to the middle ring corrugated cooling pipe 512 through the inner water inlet connecting pipe, so that the pipe cavities of the inner ring water inlet branch pipe 501 and the middle ring water inlet branch pipe 502 are communicated, forming the water delivery pipe cavity of the inner ring and the middle ring cooling pipes. Further, the outer ring water inlet branch pipe 503 corresponding to the outer ring corrugated cooling pipe 513 is communicated with the middle ring water inlet branch pipe 502 corresponding to the middle ring corrugated cooling pipe 512 through the outer water inlet connecting pipe, so that the pipe cavities of the middle ring water inlet branch pipe 502 and the outer ring water inlet branch pipe 503 are communicated, forming the water delivery pipe cavity of the outer ring and the middle ring cooling pipes. On both sides of the outer ring water inlet branch pipe 503, a first water inlet short pipe interface 506 and a second water inlet short pipe interface 507 are arranged, which are respectively connected to two pipe segments with partition barriers on the outer ring water inlet branch pipe 503 to maintain the water supply relationship to the corrugated cooling pipes 51 after grouping by partitions.

[0127] The upper water delivery pipeline includes a first upper water delivery pipeline 504 and a second upper water delivery pipeline 505. The water inlets of the first upper water delivery pipeline 504 and the second upper water delivery pipeline 505 come from the steam drum 11. The first water inlet short pipe interface 506 is connected to the first upper water delivery pipeline 504, and the second water inlet short pipe interface 507 is connected to the second upper water delivery pipeline 505, which can simultaneously deliver boiler water into the water inlet main pipe. Further, water delivery flow regulating valves are respectively arranged on the first upper water delivery pipeline 504 and the second upper water delivery pipeline 505 to maintain the controllable adjustment of the boiler water supply volume.

[0128] Similarly, from the perspective of steam output, the steam outlet main pipe includes multiple steam outlet branch pipes arranged in a ring and communicated with each other, which respectively include an inner ring steam outlet branch pipe 521, a middle ring steam outlet branch pipe 522, and an outer ring steam outlet branch pipe 523.

[0129] The blocking blocks 500 are respectively arranged corresponding to the steam outlet branch pipes to partition and isolate different steam outlet branch pipes. That is to say, two blocking blocks 500 are arranged on each of the inner-ring steam outlet branch pipe 521, the middle-ring steam outlet branch pipe 522 and the outer-ring steam outlet branch pipe 523, separating the inner-ring steam outlet branch pipe 521, the middle-ring steam outlet branch pipe 522 and the outer-ring steam outlet branch pipe 523 into two relatively independent pipe segments. In order to enable the steam outlet branch pipes at different positions to export steam to the corresponding corrugated cooling pipes 51, the steam outlet branch pipes in each partition are communicated through steam outlet connecting pipes, and the steam outlet connecting pipes are arranged in the same radial direction of the steam outlet branch pipes, enabling the steam outlet branch pipes after partition isolation to be communicated. Further, the steam outlet connecting pipes include an inner steam outlet connecting pipe arranged between the inner-ring steam outlet branch pipe 521 and the middle-ring steam outlet branch pipe 522, and an outer steam outlet connecting pipe arranged between the outer-ring steam outlet branch pipe 523 and the middle-ring steam outlet branch pipe 522, realizing the communication of the pipe cavities of the inner-ring steam outlet branch pipe 521, the middle-ring steam outlet branch pipe 522 and the outer-ring steam outlet branch pipe 523.

[0130] The inner steam outlet connecting pipe and the outer steam outlet connecting pipe are communicated with the steam outlet short pipe interfaces through the steam outlet branch pipes with partition isolation.

[0131] The inner-ring steam outlet branch pipe 521 corresponding to the inner-ring corrugated cooling pipe 511 is connected and communicated with the middle-ring steam outlet branch pipe 522 corresponding to the middle-ring corrugated cooling pipe 512 through the inner steam outlet connecting pipe, enabling the pipe cavities of the inner-ring steam outlet branch pipe 521 and the middle-ring steam outlet branch pipe 522 to be communicated and forming the steam transmission pipe cavity of the inner-ring and middle-ring cooling pipes.

[0132] Further, the outer-ring steam outlet branch pipe 523 corresponding to the outer-ring corrugated cooling pipe 513 is connected and communicated with the middle-ring steam outlet branch pipe 522 corresponding to the middle-ring corrugated cooling pipe 512 through the outer steam outlet connecting pipe, enabling the pipe cavities of the middle-ring steam outlet branch pipe 522 and the outer-ring steam outlet branch pipe 523 to be communicated and forming the steam transmission pipe cavity of the outer-ring and middle-ring cooling pipes. A first steam outlet short pipe interface 526 and a second steam outlet short pipe interface 527 are arranged on both sides of the outer-ring steam outlet branch pipe 523, and are respectively connected to the two pipe segments with partition isolation on the outer-ring steam outlet branch pipe 523, maintaining the steam export relationship of the corrugated cooling pipes 51 after being grouped by partition.

[0133] The upper steam transmission pipeline includes a first upper steam transmission pipeline 524 and a second upper steam transmission pipeline 525. The steam outlets of the first upper steam transmission pipeline 524 and the second upper steam transmission pipeline 525 are aggregated into the steam drum 11. The first steam outlet short pipe interface 526 is connected to the first upper steam transmission pipeline 524, and the second steam outlet short pipe interface 527 is connected to the second upper steam transmission pipeline 525, enabling by-products steam to be output to the steam drum 11 simultaneously.

[0134] By providing a first water flow regulating valve 52a on the first upper water conveyance pipeline 504 and a second water flow regulating valve 52b on the second upper water conveyance pipeline 505, the technical objective of simultaneous water inlet and targeted separate control of the water inlet volume can be achieved.

[0135] It should be noted that the specific number of loops of the corrugated cooling pipe 51 is not limited in this application. It can be understood that when there are more loops of corrugated heat exchange pipes, the water inlet branch pipes or steam outlet branch pipes corresponding to the multi-loop corrugated cooling pipe 51 can be spatially connected and aggregated, and an external water conveyance pipeline or steam conveyance pipeline can be connected to the steam drum 11. By combining with the setting of regulating valves on the water conveyance pipeline, the effect of targeted controllable heat transfer can also be achieved.

[0136] In this application, the number of pipe segments for partition blocking of the water inlet main pipe or the steam outlet main pipe is not limited. At the same time, referring to Figure 4 , in addition to Figure 3 the form in which the water inlet main pipe, the steam outlet main pipe, and the corrugated cooling pipe 51 are partitioned into left and right groups by the blocking block 500, it can also be partitioned into four groups in the circumferential direction, and the adjustable water supply volume corresponding to each group is controlled through the independent upper water conveyance pipeline to regulate the temperature of different regions.

[0137] To ensure sufficient catalytic oxidation reaction effect, after the reaction in the main reaction area of the upper reaction zone 5a, the remaining H2S in the sour gas continues to undergo an oxidation reaction in the lower reaction zone 5b of the catalytic oxidation reactor 5. During the reaction process, boiler water is introduced into the cooling pipes in the lower reaction zone 5b to cool the reaction bed layer, and the bed layer temperature is controlled ≤ 300 °C, so that the H2S that is not completely reacted in the upper reaction zone 5a in the sour gas can be directly oxidized by O2 into elemental sulfur.

[0138] The lower reaction zone 5b is also filled with the same catalytic oxidation catalyst 5c as the upper reaction zone 5a. Multiple straight pipe cooling pipes 53 are vertically passed through the catalyst 5c. The number of straight pipe cooling pipes 53 is determined according to the sour gas volume and composition. From the perspective that the catalytic oxidation reaction degree of the lower reaction zone 5b is lower than that of the upper reaction zone 5a, the cooling pipes in the lower reaction zone 5b are not in the form of corrugated pipes but straight pipes. The corrugated pipe has wave peaks and wave trough sections and has a larger outer surface area, which can increase the contact area with the catalytic oxidation catalyst 5c, and thus can fully ensure the cooling effect.

[0139] The cooling effect of the straight pipe form is relatively weaker than that of the corrugated pipe form, but it is more commonly used and has a lower cost. Through this setting method, based on the reaction degree of different reaction zones, the manufacturing cost of the overall equipment can be reduced, and at the same time, the basic cooling effect on the reaction bed layer can be ensured.

[0140] A plurality of straight cooling pipes 53 are arranged in an axial ring around the reactor, and both ends thereof are respectively connected to a steam header 54 located at the top of the lower reaction zone 5b and a boiler water header 55 located at the bottom of the lower reaction zone 5b.

[0141] Both the steam header 54 and the boiler water header 55 are arranged at the center inside the reactor. Further, the top and bottom ends of the straight cooling pipes 53 in the middle can be directly communicated with the steam header 54 and the water header, while the straight cooling pipes 53 outside the steam header 54 and the water header are communicated with the steam header 54 and the water header through elbow pipes located on both the top and bottom sides, which can increase the number of pipes arranged, ensure the cooling effect, and offset the defect that its cooling effect is weaker than that of the corrugated pipes.

[0142] The steam header 54 is connected to a lower steam outlet main pipe 56. The pipe orifice of the lower steam outlet main pipe 56 extends out of the reactor and is connected to the steam drum 11 through a lower steam transmission pipeline 57. The boiler water header 55 is connected to a lower water inlet main pipe 58. The lower water inlet main pipe 58 extends out of the reactor and is connected to the steam drum 11 through a lower water transmission pipeline 59. Through this setting method, it can ensure the normal water supply and normal steam supply in the lower reaction zone 5b. Similarly, through the phase change conversion of the lower water inlet, the latent heat of phase change of the boiler water is used to cool the reaction bed layer, and the by-produced steam is sent to the steam drum 11.

[0143] Through the sulfur recovery controllable heat transfer reaction device in the present invention, the reaction temperature of different bed layers inside the catalytic oxidation reactor 5 can be controlled to the greatest extent, and at the same time, a good desulfurization effect can be achieved.

[0144] Based on the above-described process flow, the present invention also provides a controllable heat transfer sulfur recovery system, including a reaction unit and a sulfur increase unit. The reaction unit includes a first acid gas preheater 1, a hydrolysis reactor 2, a second acid gas preheater 3, a third acid gas preheater 4, the above-described sulfur recovery controllable heat transfer reaction device, and connecting pipelines;

[0145] The sulfur increase unit, as another core technical point, includes an intermediate temperature condenser 6, a sulfur separator 7, a low temperature condenser 8, an adsorption reaction device 9, a tail gas detector 10, and connecting pipelines.

[0146] In the reaction unit, the cold side of the first acid gas preheater 1, the hydrolysis reactor 2, the cold side of the second acid gas preheater 3, the cold side of the third acid gas preheater 4, the catalytic oxidation reactor 5, the hot side of the second acid gas preheater 3, and the hot side of the first acid gas preheater 1 are sequentially connected through pipelines;

[0147] The hydrolysis reactor 2 is connected to a steam supply pipeline 21. An air supply pipeline 22 is connected between the hydrolysis reactor 2 and the cold side of the second sour gas preheater 3. The cold side of the first sour gas preheater 1 is connected to an intake pipeline 23. Meanwhile, the outlet branch pipeline of the cold side of the third sour gas preheater 4 is respectively connected to the downstream adsorption reaction device 9 to provide the regenerated sour gas during the regeneration process.

[0148] The first sour gas preheater 1 uses the waste heat of the reaction tail gas to heat the sour gas transported through the intake pipeline 23. After the sour gas is heated to 70°C, it enters the hydrolysis reactor 2. The hydrolysis reactor 2 is used to decompose trace organic sulfur in the sour gas and adopts a normal temperature organic sulfur hydrolysis catalyst 5c. A small amount of steam is introduced into the hydrolysis reactor 2, so that sulfides such as organic sulfur in the sour gas react with trace steam under the catalysis of the catalyst 5c to hydrolyze into H2S that is easy to remove. The reactions are as follows:

[0149] COS + H2O → H2S + CO2

[0150] CS2 + 2H2O → 2H2S + CO2

[0151] The hydrolyzed sour gas is mixed with an appropriate amount of air and then enters the second sour gas preheater 3 and the third sour gas preheater 4, where it is preheated by the waste heat of the reaction tail gas and steam to 200°C. Part of the heated sour gas enters the catalytic oxidation reactor 5 from the top, and the other part enters the adsorption reaction device 9 for regeneration.

[0152] The catalytic oxidation reactor 5 consists of a shell, a head, and internal water-cooled pipes. The catalytic oxidation catalyst 5c is filled between the water-cooled pipes and is supported by inert porcelain balls. The catalytic oxidation reactor 5 is divided into an upper reaction zone 5a and a lower reaction zone 5b. The height H1 of the upper reaction zone 5a and the height H2 of the lower reaction zone 5b are determined by the reaction rate and the amount of heat released. From another perspective, the height H1 of the upper reaction zone 5a and the height H2 of the lower reaction zone 5b can also be set according to the sour gas production scale of the established device. The number and size of the corrugated cooling pipes 51A1 - An in the upper reaction zone 5a and the straight cooling pipes 53B1 - Bn in the lower reaction zone 5b are determined by the reaction rate and the amount of heat released.

[0153] Through the above setting method, it is possible to complete the adaptive adjustment of the filling amount range of the catalyst 5c and the heat removal amount range during the design and processing stage of the catalytic oxidation reactor 5 for a device with a specific scale.

[0154] For the connection of the two system units, the outlet of the catalytic oxidation reactor 5 is connected to the hot side of the second sour gas preheater 3 to recover part of the heat of the mixed gas. The outlet of the hot side of the second sour gas preheater 3 is connected to the hot side of the first sour gas preheater 1 to continue recovering the remaining heat. The outlet of the hot side of the first sour gas preheater 1 is connected to the sulfur increase unit.

[0155] In the sulfur recovery unit, the hot side of the first acid gas preheater 1 is connected in sequence with the hot side of the medium temperature condenser 6, the sulfur separator 7, the hot side of the low temperature condenser 8, the adsorption reaction device 9 and the tail gas detector 10 through pipelines.

[0156] The hot side of the medium temperature condenser 6 is connected to the hot side outlet of the first acid gas preheater 1 to cool the tail gas to 150° C. The cooled tail gas enters the sulfur separator 7 , and the cold side of the medium temperature condenser 6 generates steam which enters the steam drum 11 .

[0157] Specifically, a medium-temperature boiler water pipeline 61 is connected to the cold side of the medium-temperature condenser 6, and steam is produced as a by-product by utilizing the heat of the remaining mixed gas in the medium-temperature condenser 6. At the same time, the tail gas passing through the first acid gas preheater 1 is condensed, and the produced steam is passed into the steam outlet main pipe connected to the steam drum 11 through the medium-temperature steam pipeline 62.

[0158] The sulfur separator 7 includes a gas-liquid separator and an internal defoaming net. In the separator, the liquid sulfur mist entrained in the gas is separated in the defoaming net, and the outlet tail gas enters the low-temperature condenser 8. The separated liquid sulfur is sent to sulfur molding. The tail gas is cooled to 50°C in the low-temperature condenser 8 and then sent to the adsorption reaction device 9.

[0159] The adsorption reaction device 9 is connected to the air inlet pipe 23 of the catalytic oxidation reactor 5 through the purge gas pipe 12, the purge gas induced draft fan 13 and the purge gas supply pipe 14 which are connected in sequence, so as to circulate the sulfur vapor generated during the regeneration process of the adsorption reaction device 9 back to the reaction unit, thereby forming a cross-correlation between the two subunits.

[0160] Through the cross-correlation of the two sub-units, the adsorbent 9c of the adsorption reaction device 9 of the sulfur recovery unit can be regenerated, and the generated elemental sulfur vapor can be circulated back to the reaction unit, so that the sulfur element can be truly recovered and finally recovered through the sulfur separator 7, forming an internal circulation of the sulfur-containing components in the system, which can ultimately ensure the desulfurization effect of the acid gas and realize the efficient recovery of sulfur.

[0161] The adsorption reaction device 9 comprises a first adsorption reactor 9a and a second adsorption reactor 9b which are arranged in parallel, and three groups of air inlet pipeline valve groups and two groups of air outlet pipeline valve groups are arranged in parallel between the first adsorption reactor 9a and the second adsorption reactor 9b;

[0162] Each set of pipeline valve groups includes a common ventilation main pipe, two branch control valves, and ventilation branches respectively connected to the first adsorption reactor 9a and the second adsorption reactor 9b.

[0163] The first adsorption reactor 9a and the second adsorption reactor 9b both include an upper adsorption zone and a lower reaction zone, and a gap is left between the upper adsorption zone and the lower reaction zone;

[0164] The height H3 of the upper adsorption zone and the height H4 of the lower reaction zone are determined by the flow rate of the sour gas. Thus, from another perspective, the upper adsorption zone and the lower reaction zone can also be set according to the sour gas production scale of the established device, and the filling amounts of the adsorbent 9c and the Claus catalyst 9d can be determined.

[0165] The upper adsorption zone is filled with the adsorbent 9c, which is mainly used to adsorb the tail gas after sulfur separation and adsorb H2S and SO2 in the tail gas; the lower reaction zone is filled with the Claus catalyst 9d. The sour gas containing H2S transported from the cold-side outlet of the upstream third sour gas preheater 4 is used to desorb H2S and SO2 in the adsorbent 9c. At the same time, the Claus reaction occurs in the lower reaction zone to be converted into elemental sulfur and then recycled and discharged back to the inlet pipeline of the catalytic oxidation reactor 5. Both the adsorbent 9c and the Claus catalyst 9d are supported by inert porcelain balls.

[0166] From the perspective of the process flow, the inlet of the adsorption reactor is connected to the low-temperature condenser 8, the third sour gas preheater 4, and the clean gas supply pipeline 18 through pipelines for adsorption and regeneration.

[0167] The tail gas from the hot side of the low-temperature condenser 8 is introduced into the adsorption reactor to adsorb the remaining H2S and SO2. When the adsorption reactor is saturated with the adsorption of H2S and SO2, it is switched to another adsorption reactor, and the sour gas from the cold-side outlet of the third sour gas preheater 4 is used to perform reduction regeneration on this reactor. The two adsorption reactors are switched cyclically.

[0168] Two parallel adsorption reactors, and three groups of inlet pipeline valve groups and two groups of outlet pipeline valve groups arranged between the adsorption reactors are mainly used for the switching between adsorption and regeneration.

[0169] From the perspective of one adsorption and one regeneration when the two adsorption reactors are operating simultaneously, the outlets of the two adsorption reactors are respectively connected to the main ventilation pipe for outputting clean gas, which is used for detection and external discharge through the tail gas detector 10, and for circulating and returning the clean gas for purging and cooling the regenerated adsorption reactor for purging.

[0170] And the two adsorption reactors are respectively connected to the main ventilation pipe for discharging the purging gas, which is used for circulating and returning the sulfur vapor and the purging gas generated by the Claus reaction during the regeneration process to the inlet pipeline of the catalytic oxidation reactor 5.

[0171] The SO2 emission concentration in the tail gas after adsorption is less than 10mg / Nm 3 , and the H2S emission concentration is less than 0.03mg / Nm 3 .

[0172] The regenerated sour gas containing H2S comes from the hydrolysis reactor 2. During the regeneration process, the operating temperature of the Claus catalyst 9d is maintained at 320°C - 400°C, which can promote the Claus reaction and maximize the regeneration of SO2. The reaction that occurs is:

[0173] 2H2S + SO2 → 3S + 2H2O

[0174] The regenerated gas returns to the inlet of the catalytic oxidation reactor 5. After regeneration, the adsorption reactor is purged with clean gas and cooled for standby.

[0175] Specifically, the outlet pipeline valve group includes the first outlet pipeline valve group 91 and the second outlet pipeline valve group 92; the first outlet pipeline valve group 91 is used to output clean gas. The tail gas detector 10 is connected to the clean gas exhaust pipeline 15 connected to the ventilation main pipe of the first outlet pipeline valve group 91, and a clean gas extraction pipeline 16 is connected to the clean gas exhaust pipeline 15 upstream of the tail gas detector 10. The clean gas extraction pipeline 16 is connected to a clean gas extraction fan 17, and the clean gas extraction fan 17 is connected to the ventilation main pipe of one group of inlet pipeline valve groups through a clean gas supply pipeline 18. In this pipeline valve group, there are a seventh control valve V7 and an eighth control valve V8, corresponding to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

[0176] The second outlet pipeline valve group 92 is used to internally circulate and export the purge gas during regeneration and purging. The root of the purge gas pipeline 12 is connected to the ventilation main pipe of the second outlet pipeline valve group 92. In this pipeline valve group, there are a ninth control valve V9 and a tenth control valve V10, corresponding to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

[0177] The inlet pipeline valve group includes the first inlet pipeline valve group 93, the second inlet pipeline valve group 94, and the third inlet pipeline valve group 95.

[0178] The first inlet pipeline valve group 93 is used to introduce the regenerated sour gas. The ventilation main pipe is connected to the cold side of the third sour gas preheater 4 through a pipeline. In this pipeline valve group, there are a first control valve V1 and a second control valve V2, corresponding to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

[0179] The second inlet pipeline valve group 94 is used to introduce the tail gas after sulfur separation for adsorbing H2S and SO2 in the tail gas. The ventilation main pipe is connected to the hot side of the low-temperature condenser 8 through a pipeline. In this pipeline valve group, there are a third control valve V3 and a fourth control valve V4, corresponding to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

[0180] The third intake air pipeline valve group 95 is used to introduce clean gas for purging. The clean gas supply pipeline 18 is connected to the ventilation main pipe of the third intake air pipeline valve group 95. In this pipeline valve group, there are a fifth control valve V5 and a sixth control valve V6, corresponding to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

[0181] During the specific operation process, combined with Figure 1 , it is illustrated with a specific example:

[0182] The tail gas from the low-temperature condenser 8 first enters the first adsorption reactor 9a to adsorb the remaining H2S and SO2. At this time, the third control valve V3 and the seventh control valve V7 are opened, while the first control valve V1, the fourth control valve V4, the fifth control valve V5, the eighth control valve V8, and the ninth control valve V9 are closed. At the same time, the second control valve V2, the sixth control valve V6, and the tenth control valve V10 are opened, enabling the first adsorption reactor 9a to perform adsorption and the second adsorption reactor 9b to perform regeneration.

[0183] The tail gas at the outlet of the first adsorption reactor 9a is detected online by the tail gas detector 10. When the H2S concentration reaches 0.03 mg / Nm 3 or the SO2 concentration reaches 10 mg / Nm 3 , it is switched to the second adsorption reactor 9b for adsorption. At this time, the second control valve V2, the third control valve V3, the sixth control valve V6, the seventh control valve V7, and the tenth control valve V10 are closed. At the same time, the fourth control valve V4 and the eighth control valve V8 are opened, enabling the second adsorption reactor 9b to perform adsorption and the first adsorption reactor 9a to perform regeneration.

[0184] The acid gas from the third acid gas preheater 4 enters the first adsorption reactor 9a for regeneration. At this time, the first control valve V1 and the ninth control valve V9 are opened. The H2S in the acid gas reacts with the desorbed H2S / SO2 under the action of the catalyst 5c to generate elemental sulfur. The temperature of the first adsorption reactor 9a is maintained at 320°C - 400°C. The desorbed mixed gas is mixed with the acid gas at the inlet of the catalytic oxidation reactor 5 and enters the catalytic oxidation reactor 5. After the regeneration is completed, the first control valve V1 is closed and the fifth control valve V5 is opened. The first adsorption reactor 9a is purged with clean tail gas, cooled down, and standby for the next adsorption. After the purging is completed, the fifth control valve V5 and the ninth control valve V9 are closed.

[0185] When the H2S concentration at the outlet of the second adsorption reactor 9b reaches 0.03 mg / Nm 3 or the SO2 concentration reaches 10 mg / Nm 3When it is time to switch to the adsorption process of the first adsorption reactor 9a, the second adsorption reactor 9b enters the regeneration process, and the switching is cycled in turn. Through the setting of the above control valves, the switching between adsorption and regeneration can be carried out to ensure the stable and reliable normal tail gas adsorption and desorption regeneration.

[0186] In one specific application example, the flow rate of the sour gas generated by an upstream device is 20,000 Nm³ / h, and the composition is: 60% CO2, 15% H2S, 25% N2, and COS ≤ 25 mg / m³.

[0187] The sour gas is heated to 70°C by the first sour gas preheater 1 and then enters the hydrolysis reactor 2. The catalyst 5c loading in the hydrolysis reactor 2 is 20 m³. In the catalytic action of the catalyst 5c, organic sulfur such as COS in the mixed gas reacts with trace water vapor to hydrolyze into H2S that is easy to remove. Subsequently, it is mixed with 7150 Nm³ / h of air and enters the second sour gas preheater 3 and the third sour gas preheater 4 in turn, and is preheated to 200°C by the reaction gas and steam. Part of the mixed gas enters the catalytic oxidation reactor 5 from the top, and the other part is used for the regeneration of the adsorption reactor in the sulfur increase unit.

[0188] The mixed gas enters the upper reaction zone 5a from the top of the catalytic oxidation reactor 5. The upper reaction zone 5a is filled with the catalytic oxidation catalyst 5c, and the loading is 20 m³. The inlet of the corrugated cooling tube 51 is connected to the water inlet main pipe arranged annularly along the reactor, and the outlet of the corrugated cooling tube 51 converges into the steam outlet main pipe arranged annularly along the reactor. Under the action of the catalyst 5c, H2S reacts with oxygen to generate elemental sulfur and produce a small amount of SO2. The temperature of the reaction zone is controlled ≤ 300°C by cooling through the corrugated cooling tube 51 arranged in the upper reaction zone 5a, and the by-product steam is 6.2 t / h. The steam enters the steam drum 11, and the remaining unreacted sour gas enters the lower reaction zone 5b.

[0189] The lower reaction zone 5b is filled with the catalytic oxidation catalyst 5c, and the loading is 30 m³. The straight pipe cooling tube 53 is set. The upper end of the straight pipe cooling tube 53 is connected to the steam header 54 arranged in the center, converges into the steam outlet main pipe, and the lower end is connected to the boiler water header 55 arranged in the center, converges into the water inlet main pipe. The steam outlet main pipe and the water inlet main pipe are respectively connected to the external steam drum 11. Under the action of the catalyst 5c, the remaining H2S reacts with oxygen to generate elemental sulfur and produce a small amount of SO2. The temperature of the reaction zone is controlled ≤ 300°C by cooling through the straight pipe cooling tube 53 arranged in the lower reaction zone 5b, and the by-product steam is 3.4 t / h. The steam enters the steam drum 11. The H2S concentration in the mixed gas at the outlet of the catalytic oxidation reactor 5 is < 0.01%, and the SO2 concentration is < 0.1%.

[0190] The mixed gas enters the second sour gas preheater 3 to recover part of the heat, then enters the first sour gas preheater 1 to recover the remaining heat, and finally enters the medium-temperature condenser 6 to recover the remaining heat, with the temperature dropping to 150°C. The cooled mixed gas enters the sulfur separator 7. Through the internal demisting mesh, the liquid sulfur mist entrained in the mixed gas in the sulfur separator 7 is separated out by the demisting mesh. The tail gas at the upper outlet of the sulfur separator 7 enters the low-temperature condenser 8, and the liquid sulfur separated at the lower outlet of the sulfur separator 7 is sent for sulfur forming. The sulfur recovery is 4291 kg / h, and the sulfur recovery rate is 99.9%. After the tail gas is cooled to 50°C in the low-temperature condenser 8, it is sent to the sulfur enrichment unit. The SO2 emission concentration in the clean gas after being treated by the sulfur enrichment unit is lower than 10 mg / Nm 3 , and the H2S emission concentration is lower than 0.03 mg / Nm 3 .

[0191] Through the sulfur recovery controllable heat transfer reaction device and the sulfur recovery system in this application, effective desulfurization treatment can be carried out for low-concentration H2S sour gas. It can be applied to the treatment of sour gas with an H2S concentration of 1% - 15% in the form of controllable heat transfer. By adjusting the reaction temperature, the treatment of sour gas with different H2S contents in the low-concentration range can be achieved, and sulfur enrichment can be realized.

[0192] It should be noted that, without conflict, the features in the embodiments of this application can be combined with each other.

[0193] The above are only the preferred embodiments of this application and are not used to limit this application. For those skilled in the art, this application can have various changes and modifications. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of this application shall be included in the protection scope of this application.

Claims

1. A controllable heat transfer sulfur recovery system, characterized in that: It comprises a reaction unit and a sulfur yield increasing unit, wherein the reaction unit comprises a first acid gas preheater, a hydrolysis reactor, a second acid gas preheater, a third acid gas preheater, a controllable heat transfer reaction device and a connecting pipeline; The sulfur yield increasing unit comprises a medium temperature condenser, a sulfur separator, a low temperature condenser, an adsorption reaction device, a tail gas detector and connecting pipes; The controllable heat transfer reaction device comprises a catalytic oxidation reactor and a steam drum, wherein the catalytic oxidation reactor comprises an upper reaction zone; The cold side of the first acid gas preheater, the hydrolysis reactor, the cold side of the second acid gas preheater, the cold side of the third acid gas preheater, the catalytic oxidation reactor, the hot side of the second acid gas preheater and the hot side of the first acid gas preheater are sequentially connected by pipelines; The hot side of the first acid gas preheater, the hot side of the medium temperature condenser, the sulfur separator, the hot side of the low temperature condenser, the adsorption reaction device and the tail gas detector are connected in sequence through pipelines; The adsorption reaction device is connected to the air inlet pipe of the catalytic oxidation reactor through a purge air pipe, a purge air induced draft fan and a purge air delivery pipe which are connected in sequence; The adsorption reaction device comprises a first adsorption reactor and a second adsorption reactor which are arranged in parallel, wherein the first adsorption reactor and the second adsorption reactor each comprise an upper adsorption zone and a lower reaction zone, and a gap is left between the upper adsorption zone and the lower reaction zone; The upper adsorption zone is filled with an adsorbent, and the lower reaction zone is filled with a Claus catalyst; The upper reaction zone is filled with a catalyst, and a plurality of corrugated cooling pipes are vertically connected through the catalyst. The plurality of corrugated cooling pipes are arranged in a ring around the axial direction of the reactor to form a plurality of rings of corrugated cooling pipes from the inside to the outside along the radial direction of the reactor. The number of the corrugated cooling pipes is determined according to the amount and composition of the acid gas. The top ends of the corrugated cooling pipes are connected to a steam outlet main pipe arranged in an annular manner at the top of the upper reaction zone, and the bottom ends of the corrugated cooling pipes are connected to a water inlet main pipe arranged in an annular manner at the bottom of the upper reaction zone; The water inlet main pipe is partitioned and blocked by a blocking block, and the steam outlet main pipe is partitioned and blocked by a blocking block, and the corrugated cooling pipes corresponding to each partition are arranged in groups; The water inlet main pipes arranged in different zones are connected with water inlet short pipe interfaces, and the water inlet short pipe interfaces are connected with the steam drum through external upper water delivery pipelines, and the upper water delivery pipelines are respectively provided with water delivery flow regulating valves; The steam outlet main pipes arranged in different zones are connected with corresponding steam outlet short pipe interfaces, and the steam outlet short pipe interfaces are connected to the steam drum through external upper steam transmission pipelines; The setting position of the blocking block on the water inlet main pipe corresponds to the setting position of the blocking block on the steam outlet main pipe in the upper and lower directions; The steam drum is connected with a boiler water delivery pipeline, and a boiler water flow regulating valve is arranged on the boiler water delivery pipeline.

2. The controllable heat transfer sulfur recovery system according to claim 1, characterized in that: The water inlet flow rate of the upper water delivery pipeline is regulated by the water delivery flow regulating valve, and the water inlet flow rate is controlled according to the outlet temperature of the catalytic oxidation reactor.

3. The controllable heat transfer sulfur recovery system according to claim 1, characterized in that: The water inlet main pipe includes a plurality of water inlet branch pipes which are arranged in an annular manner and are interconnected, including an inner ring water inlet branch pipe, a middle ring water inlet branch pipe and an outer ring water inlet branch pipe; The blocking blocks are respectively arranged on the water inlet branch pipes to isolate different water inlet branch pipes; The water inlet branch pipes of each partition are connected through a water inlet connecting pipe, and the water inlet connecting pipe is arranged in the same radial direction of the water inlet branch pipes; The water inlet connecting pipe comprises an inner water inlet connecting pipe arranged between the inner ring water inlet branch pipe and the middle ring water inlet branch pipe, and an outer water inlet connecting pipe arranged between the outer ring water inlet branch pipe and the middle ring water inlet branch pipe; The inner water inlet connecting pipe and the outer water inlet connecting pipe are connected to the water inlet short pipe interface through the water inlet branch pipe blocked by the partition.

4. The controllable heat transfer sulfur recovery system according to claim 3 is characterized in that: The steam outlet main pipe comprises a plurality of steam outlet branch pipes which are arranged in an annular manner and are interconnected, and respectively comprise an inner ring steam outlet branch pipe, a middle ring steam outlet branch pipe and an outer ring steam outlet branch pipe; The blocking blocks are respectively arranged on the steam outlet branch pipes to block the different steam outlet branch pipes in different areas; The steam outlet branch pipes of each partition are connected through a steam outlet connecting pipe, and the steam outlet connecting pipe is arranged in the same radial direction of the steam outlet branch pipes; The steam outlet connecting pipe comprises an inner steam outlet connecting pipe arranged between the inner ring steam outlet branch pipe and the middle ring steam outlet branch pipe, and an outer steam outlet connecting pipe arranged between the outer ring steam outlet branch pipe and the middle ring steam outlet branch pipe; The inner steam outlet connecting pipe and the outer steam outlet connecting pipe are connected to the steam outlet short pipe interface through the steam outlet branch pipe blocked by partitions.

5. The controllable heat transfer sulfur recovery system according to claim 1, characterized in that: The catalytic oxidation reactor also includes a lower reaction zone, which is filled with a catalyst, and a plurality of straight cooling pipes are vertically penetrated through the catalyst, and the plurality of straight cooling pipes are arranged in an annular manner around the axial direction of the reactor, and the number of the straight cooling pipes is determined according to the amount and composition of the acidic gas, and the two ends of the straight cooling pipes are respectively connected to a steam header located at the top of the lower reaction zone and a boiler water header located at the bottom of the lower reaction zone, the steam header is connected to a lower steam outlet main pipe, the pipe mouth of the lower steam outlet main pipe extends out of the reactor and is connected to the steam drum through a lower steam transmission pipeline, and the boiler water header is connected to a lower water inlet main pipe, the lower water inlet main pipe extends out of the reactor and is connected to the steam drum through a lower water transmission pipeline; The number and pipe sizes of the corrugated cooling pipes and the straight cooling pipes correspond to the reaction rates and heat release of the upper reaction zone and the lower reaction zone, respectively.

6. The controllable heat transfer sulfur recovery system according to claim 1, characterized in that: The hydrolysis reactor is connected to a steam supply pipeline, an air supply pipeline is connected between the hydrolysis reactor and the cold side of the second acid gas preheater, and the cold side of the first acid gas preheater is connected to an air intake pipeline.

7. The controllable heat transfer sulfur recovery system according to claim 1, characterized in that: The cold side of the medium-temperature condenser is connected to a medium-temperature boiler water pipeline, and the produced steam is passed into the steam outlet main pipe connected to the steam drum through a medium-temperature steam pipeline.

8. The controllable heat transfer sulfur recovery system according to claim 7, characterized in that: Three groups of air inlet pipeline valve groups and two groups of air outlet pipeline valve groups are arranged in parallel between the first adsorption reactor and the second adsorption reactor; Each set of pipeline valve groups includes a common ventilation main pipe, two branch control valves and ventilation branches respectively connected to the first adsorption reactor and the second adsorption reactor.

9. The controllable heat transfer sulfur recovery system according to claim 8, characterized in that: The air outlet pipeline valve group includes a first air outlet pipeline valve group and a second air outlet pipeline valve group; The first air outlet pipeline valve group is used to output clean air, the exhaust gas detector is connected to a clean air discharge pipeline connected to a ventilation main pipe having the first air outlet pipeline valve group, and a clean air bleed pipeline is connected to the clean air discharge pipeline upstream of the exhaust gas detector, the clean air bleed pipeline is connected to a clean air induced draft fan, and the clean air induced draft fan is connected to the ventilation main pipe of one group of air inlet pipeline valve groups through a clean air supply pipeline; The second gas outlet pipeline valve group is used for internal circulation to derive the purge gas, and the root of the purge gas pipeline is connected to the ventilation main pipe of the second gas outlet pipeline valve group; The air intake pipeline valve group includes a first air intake pipeline valve group, a second air intake pipeline valve group and a third air intake pipeline valve group, the first air intake pipeline valve group is used to introduce regenerated acid gas, and the ventilation main pipe is connected to the cold side of the third acid gas preheater through a pipeline; The second air inlet pipeline valve group is used to introduce tail gas after sulfur separation, and the ventilation main pipe is connected to the hot side of the low-temperature condenser through a pipeline; The third air intake pipeline valve group is used to introduce clean air for purging, and the clean air supply pipeline is connected to the ventilation main pipe of the third air intake pipeline valve group.

10. The controllable heat transfer sulfur recovery system according to claim 8, characterized in that: The adsorbent and the Claus catalyst are both supported by inert ceramic balls.

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