Controllable heat transfer sulfur recovery system

Abstract

The invention relates to a controllable heat transfer sulfur recovery system which comprises a reaction unit and a sulfur yield increasing unit, and the reaction unit comprises a controllable heat transfer reaction device and a connecting pipeline; the controllable heat transfer reaction device comprises a catalytic oxidation reactor and a steam pocket, a multi-ring wave node cooling pipe is arranged in the catalytic oxidation reactor, the top end and the bottom end of the wave node cooling pipe are gathered on a steam outlet header pipe and a water inlet header pipe respectively, and the water inlet header pipe is connected with the steam pocket through an external upper water conveying pipeline. Water delivery flow regulating valves are respectively arranged on the upper water delivery pipelines; and a boiler water flow regulating valve is arranged on a boiler water conveying pipeline connected with the steam pocket. According to the invention, the sulfur component in the acid gas can be recovered to the greatest extent, and no residue is generated in the tail gas, so that the up-to-standard emission of the tail gas is ensured. And meanwhile, through a controllable heat transfer recovery system, energy recovery is achieved, and a byproduct is steam.

Description

Technical Field

[0001] The present application relates to a desulfurization and purification device for acid gas in production processes such as coal chemical industry and natural gas engineering, and more specifically, 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, and selective catalytic oxidation sulfur recovery processes.

[0003] Sulfur recovery by molten sulfur: H2S is absorbed by the liquid phase and then reacts with O2 in the air to generate elemental sulfur. The sulfur is separated by flotation in the jet regeneration tank to form sulfur foam. The sulfur foam flows into the molten sulfur kettle through the intermediate tank. The molten sulfur kettle is heated by external steam to make the sulfur molten, and then the water is separated to recover the sulfur paste. The main disadvantage of this method is the low sulfur recovery efficiency (less than 90%). The use of this method to recover sulfur from acidic gas in large-scale chemical production equipment cannot meet environmental protection requirements.

[0004] Conventional Claus reaction technology: Different from low-temperature Claus reaction, it refers to Claus reaction carried out under the condition of higher sulfur dew point temperature, and sulfur separation device is set after the reactor. Due to the high reaction temperature, the reaction equilibrium is not conducive to the direction of sulfur generation, so the sulfur recovery rate is below 98% compared with low-temperature Claus technology.

[0005] Low-temperature Claus technology: refers to the Claus reaction carried out under the condition of temperature lower than the sulfur dew point. The characteristic of this tail gas treatment method is that 2~3 low-temperature converters are configured after the sulfur recovery device, and the reaction temperature is about 130℃. Due to the low reaction temperature, the reaction equilibrium shifts greatly toward the direction of sulfur generation, and part of the generated liquid sulfur is immediately deposited on the catalyst, so the converter needs to be periodically regenerated and switched for use, and its sulfur recovery rate can reach more than 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 process is no longer applicable. It is even more difficult to handle lean acid gas or tail gas with an H2S content lower than 5% (V). For example, the H2S content of MDEA desulfurization regeneration gas used in the desulfurization of oil field associated gas and coal-to-syngas is 2~5%, and its sulfur recovery cannot be completely recovered, so the tail gas needs to rely on incineration for desulfurization. Similarly, the H2S content of NHD desulfurization regeneration gas used in the desulfurization of coal-to-syngas is 2~5%, and the same problem also exists.

[0007] In order to overcome the problem that when the H2S content in acid gas is lower than 15% (V), molten sulfur recovery technology, Claus technology, and conventional catalytic oxidation sulfur recovery no longer meet the current environmental emission requirements. Therefore, it is necessary to seek to develop a sulfur recovery process to solve the problem when the H2S content in acid gas is lower than 15% (V), and this process must fully meet environmental 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, which provides a catalytic oxidation reactor to make it suitable for acid gas with H2S concentration of 1%-15%. By setting up a yield increase system, the desulfurization accuracy and sulfur recovery rate are improved to ensure that the tail gas meets the emission standards. At the same time, through the controllable heat transfer system, energy recovery is achieved and steam is produced as a by-product.

[0009] In order to achieve the above-mentioned object, the present invention provides a controllable heat transfer sulfur recovery system, comprising a reaction unit and a sulfur recovery 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;

[0010] 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;

[0011] 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;

[0012] 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.

[0013] 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;

[0014] 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;

[0015] 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;

[0016] 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;

[0017] 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;

[0018] 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.

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

[0020] In an optional embodiment, 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;

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

[0022] 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;

[0023] 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;

[0024] 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.

[0025] In an optional embodiment, the steam outlet main pipe includes a plurality of steam outlet branch pipes which are arranged in an annular manner and are interconnected, 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 blocking blocks are respectively arranged on the steam outlet branch pipes to block the different steam outlet branch pipes in different areas;

[0027] 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;

[0028] 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;

[0029] 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.

[0030] In an optional embodiment, the catalytic oxidation reactor further comprises a lower reaction zone, the lower reaction zone is filled with a catalyst, a plurality of straight cooling tubes are vertically penetrated through the catalyst, the plurality of straight cooling tubes are arranged in an axial ring around the reactor, the number of the straight cooling tubes is determined according to the amount and composition of the acidic gas, and the two ends of the straight cooling tubes 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, 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;

[0031] 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.

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

[0033] 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.

[0034] In an optional 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 connected in sequence through pipelines;

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

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

[0037] In an optional embodiment, the adsorption reaction device includes a first adsorption reactor and a second adsorption reactor 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 and the second adsorption reactor;

[0038] 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.

[0039] In an optional embodiment, the gas outlet pipeline valve group includes a first gas outlet pipeline valve group and a second gas outlet pipeline valve group;

[0040] The first air outlet pipeline valve group is used to output clean air, the exhaust gas detector is connected to the clean air discharge pipeline connected to the ventilation main pipe of the first air outlet pipeline valve group, and the clean air discharge pipeline upstream of the exhaust gas detector is connected to a clean air bleed pipeline, 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 the air inlet pipeline valve groups through a clean air supply pipeline;

[0041] 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;

[0042] 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;

[0043] 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;

[0044] 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.

[0045] In an optional embodiment, the first adsorption reactor and the second adsorption reactor each 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;

[0046] The upper adsorption zone is filled with an adsorbent, and the lower reaction zone is filled with a 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 the present application, low-concentration H2S acid gas with an H2S content of less than 15% (V) can be effectively treated, and the temperature of the reaction zone in the catalytic oxidation reactor is controlled in the form of controllable heat transfer, thereby adapting to the treatment requirements of acid gas with different H2S concentrations and achieving the purpose of controllable heat transfer.

[0048] At the same time, the controllable heat transfer in the reaction zone can adapt to the treatment of acid gas with different inlet amounts, so as to reduce the impact of fluctuations in the amount of acid gas discharged from the upstream device on the desulfurization treatment effect.

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

[0050] The sulfur recovery system can achieve efficient sulfur recovery, improve the desulfurization accuracy of acid gas and the sulfur recovery rate, and ensure that tail gas emissions meet standards.

[0051] At the same time, the sulfur recovery system of the present invention can recover the sulfur components in the acid gas to the maximum extent and ensure that no residue is generated in the tail gas, thereby ensuring that the tail gas is discharged in compliance with the emission standards.

[0052] By controllably transferring heat from the core reaction area of ​​the catalytic oxidation reactor, the heat released during the catalytic oxidation reaction can be recovered in the form of cooling, thereby achieving energy recovery and producing steam as a by-product.

[0053] Other features and advantages of the present application will be described in detail in the subsequent detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0054] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings required for use in the embodiments will be briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present application and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without paying creative work.

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

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

[0057] Figure 3 A schematic diagram of the arrangement structure of a corrugated cooling tube in one form of partitioning in the upper reaction zone;

[0058] Figure 4It is a schematic diagram of another type of partitioning arrangement of the corrugated cooling tube in the upper reaction zone;

[0059] Figure 5 It is a schematic diagram of the arrangement structure of the straight tube cooling tube in the lower reaction zone;

[0060] Figure 6 It is a structural schematic diagram of a corrugated cooling tube;

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

[0062] icon:

[0063] 1-First acid gas preheater;

[0064] 2-hydrolysis reactor; 21-steam supply pipeline; 22-air supply pipeline; 23-air intake 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-blocking 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 transmission pipeline; 525-second upper steam transmission 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 tube cooling pipe; 54-steam header; 55-boiler water header; 56-lower steam outlet main pipe; 57-lower steam transmission pipeline; 58-lower water inlet main pipe; 59-lower water transmission pipeline;

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

[0074] 7-Sulfur separator; 8-Cryogenic condenser;

[0075] 9-adsorption reaction device; 9a-first adsorption reactor; 9b-second adsorption reactor; 9c-adsorbent; 9d-Claus catalyst; 91-first outlet pipeline valve group; 92-second outlet pipeline valve group; 93-first inlet pipeline valve group; 94-second inlet pipeline valve group; 95-third inlet pipeline valve group; 10-tail gas detector; 11-steam drum; 12-purge gas pipeline; 13-purge gas induced draft fan; 14-purge gas delivery pipeline; 15-clean gas external exhaust pipeline; 16-clean gas induced draft pipeline; 17-clean gas induced draft fan; 18-clean gas delivery 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 DESCRIPTION

[0077] In order to make the purpose, technical scheme and advantages of the embodiments of the present application clearer, the technical scheme in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, rather than all of the embodiments. The components of the embodiments of the present application described and shown in the drawings here can be arranged and designed in various different configurations.

[0078] In the description of this application, it should be noted that the terms "inside", "outside", etc. indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, or the orientation or positional relationship in which the product of the application is usually placed when in use, which is only for the convenience of describing this application and simplifying the description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on this application. In addition, the terms "first", "second", etc. are only used to distinguish the description, 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 "disposed" and "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 a direct connection, or an indirect connection through an intermediate medium, or it can be the internal communication of two elements. For ordinary technicians in this field, 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 the present application is mainly used in the desulfurization treatment and sulfur recovery of low-concentration H2S acid gas with an H2S content of less than 15% (V) in the acid gas. Specifically, by changing the structure of the reaction device and setting a sulfur recovery system, the controllable heat transfer and sulfur recovery of the catalytic oxidation reactor are realized, ensuring that the 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 controllable heat transfer reaction device and sulfur recovery system are mainly reflected in the two key technical points of controllable heat transfer and sulfur recovery. At the same time, through the mutual cooperation of the reaction unit and the sulfur recovery unit, a synergistic cross-correlation is formed between the desulfurization treatment and the sulfur recovery, which ultimately ensures that a relatively high desulfurization accuracy and sulfur recovery rate are maintained.

[0082] See also Figure 1 , and combined with Figure 2 as well as Figure 7 Before describing the technical solution in this application in detail, a brief description of the desulfurization and sulfur recovery system in this application is given as a whole at the process level.

[0083] The low-concentration H2S acid gas transported from the upstream is first heated by the waste heat of the downstream reaction tail gas. After the temperature is raised, it enters the hydrolysis reactor 2 and reacts with trace steam to be hydrolyzed, so that organic sulfur such as COS and CS2 in the acid gas is hydrolyzed to generate H2S that is easy to remove.

[0084] After the acid gas after hydrolysis is mixed with an appropriate amount of air, it continues to be heated using the waste heat of the downstream reaction tail gas. After the temperature is raised, part of it undergoes catalytic oxidation reaction, and the other part is used to regenerate the downstream adsorption reactor.

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

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

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

[0088] At the same time, the regeneration gas containing H2S obtained after upstream hydrolysis is used to desorb the adsorbent 9c saturated with SO2 adsorption, and after a regeneration reaction through the Claus catalyst 9d, the sulfur element produced in the regeneration process is circulated in the regenerator back to sulfur recovery.

[0089] From the perspective of acid gas catalytic oxidation, combined with Figure 1-Figure 6 One of the core technical points of the present invention is to provide a controllable heat transfer reaction device, including a catalytic oxidation reactor 5 and a steam drum 11, wherein 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 is carried out in the upper reaction zone 5a. That is to say, the upper reaction zone 5a belongs to the main reaction area. The present application is mainly used to control the reaction temperature of the upper reaction zone 5a to perform controllable heat transfer.

[0091] The upper reaction zone 5a is filled with a catalytic oxidation catalyst 5c, which is supported by inert porcelain balls. The filled catalytic oxidation catalyst 5c constitutes the catalyst 5c bed 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 with most of the H2S removed enters the lower reaction zone 5b, and the remaining H2S is directly oxidized by O2 into elemental sulfur. Heat exchange tubes are provided in the catalyst 5c beds of the upper reaction zone 5a and the lower reaction zone 5b. The bed temperature is controlled to be ≤300°C by passing boiler water into the heat exchange tubes to cool the bed temperature. The reaction is:

[0092]

[0093]

[0094] In order to controllably transfer heat to the main reaction area of ​​the upper reaction zone 5a, a plurality of corrugated cooling tubes 51 are vertically connected through the catalyst 5c. The plurality of corrugated cooling tubes 51 constitute the cooling tubes of the upper reaction zone 5a. Furthermore, the plurality of corrugated cooling tubes 51 are arranged in an axial ring around the reactor to form a multi-ring corrugated cooling tube 51 from the inside to the outside along the radial direction of the reactor. The number of the corrugated cooling tubes 51 is determined according to the amount and composition of the acidic gas.

[0095] Specifically, the top ends of each ring of corrugated cooling tubes 51 are respectively connected to the annular steam outlet main pipe located at the top of the upper reaction zone 5a, and the bottom ends of each ring of corrugated cooling tubes 51 are respectively connected to the annular water inlet main pipe located at the bottom of the upper reaction zone 5a.

[0096] That is to say, each ring of corrugated cooling tube 51 is provided with a steam outlet main pipe and a water inlet main pipe arranged in a ring on both sides of the top and bottom, and 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 tube 51 through the water inlet main pipe located at the bottom. The boiler water flows from bottom to top and uses the latent heat of evaporation to cool the reaction bed during the flow. At the same time, the boiler water itself changes phase and is converted into steam and collected to the steam outlet main pipe located at the top, thereby returning the steam to the steam drum 11.

[0098] With reference to the accompanying drawings, the corrugated cooling tube 51 in the present application includes an inner ring corrugated cooling tube 511 , a middle ring corrugated cooling tube 512 and an outer ring corrugated cooling tube 513 , and the catalytic oxidation catalyst 5c is loaded between the multi-ring corrugated cooling tubes 51 .

[0099] Through the multi-ring arrangement of the corrugated cooling tubes 51, the cooling tubes of different ring groups can correspond to different radial positions of the main reaction area, thereby maintaining sufficient coverage of the reaction area.

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

[0101] The adjustment of the reaction temperature is mainly carried out by controlling and regulating the feed amount of boiler water in the water inlet main.

[0102] At the same time, in order to achieve controllable heat transfer of reaction temperatures in different reaction areas of the upper reaction zone 5a, the water inlet main pipe and the steam outlet main pipe are divided into zones to achieve grouping of different corrugated cooling tubes 51 in the upper reaction zone 5a.

[0103] Specifically, the water inlet main pipe is partitioned and blocked by blocking blocks 500, and the corrugated cooling pipes 51 corresponding to each partition are arranged in groups. The partitioned water inlet main pipe is connected with a corresponding water inlet short pipe interface, which is connected to the steam drum 11 through an external upper water supply pipeline, and a water supply flow regulating valve is respectively arranged on each upper water supply pipeline, so as to realize the water supply adjustment of the boiler water flow in the corrugated cooling pipes 51 grouped in each partition.

[0104] Furthermore, the pipe section of the water inlet main of each zone corresponds to an upper water supply pipeline, and the water supply flow regulating valve on each upper water supply pipeline is independently controlled, so that the overall flow of the boiler water feed can be kept stable, and the water supply of the boiler water feed can be increased or decreased at the same time.

[0105] Specifically, the water inlet flow rate of the upper water supply pipe is regulated by a water supply flow regulating valve, and the water inlet flow rate is controlled according to the outlet temperature of the catalytic oxidation reactor 5. In detail, a temperature sensor is provided on the outlet pipe of the catalytic oxidation reactor 5, and the temperature sensor and the water supply flow regulating valve are respectively electrically connected to the control system to establish a temperature flow control loop, and the boiler water inlet flow rate is controlled and regulated according to the gas temperature at the outlet of the catalytic oxidation reactor 5.

[0106] The control adjustment angle can be used to maintain the same flow rate of boiler water in the upper water supply pipe corresponding to each partitioned section of the water inlet main pipe, and the flow rate of boiler water in each upper water supply pipe can be increased or decreased synchronously. This operating condition corresponds to the ups and downs of the amount of acid gas entering the upper reaction zone 5a.

[0107] At the same time, different boiler water flow rates in the upper water supply pipeline corresponding to each partitioned section of the water inlet main can be maintained, and the boiler water flow rate in each upper water supply pipeline can be independently increased or decreased. This operating condition corresponds to controllable heat transfer adjustment for different reaction zones of the bed.

[0108] Specifically, combined with Figure 3 In the embodiment, the water inlet main pipe is divided into left and right partitions by a blocking block 500, and the multi-ring distributed corrugated cooling pipes 51 are arranged in the form of two left and right groups, forming a water inlet form of the upper water supply pipeline to the left and right sides of the catalytic oxidation reactor 5, which can specifically control and adjust the reaction conditions of the catalyst 5c in different parts of the reactor, thereby adjusting the use of the catalyst 5c in the above-mentioned different areas. The adjustment of the use of the catalyst 5c can be understood as a targeted switching protection of the operating condition of the catalyst 5c.

[0109] For example, when most of the acid gas enters the reactor through the gap between the top steam outlet mains, the catalyst 5c bed on the left side can be cooled down to a large extent by increasing the flow rate of boiler water in the upper water supply pipe on the left side, while controlling and maintaining the minimum flow rate in the upper water supply pipe on the right side to avoid the corrugated cooling pipe 51 on the right side of the reactor from being thermally damaged. In other words, the minimum flow rate is set corresponding to the diameter and length of the corrugated cooling pipe 51, which can comprehensively consider the worst working conditions of the corrugated cooling pipe 51 and minimize the impact of thermal damage to the corrugated cooling pipe 51.

[0110] Combined with the transfer of heat in the entire reaction bed, the bed temperature can be controlled to ≤300°C, on the premise that H2S in different reaction zones can be directly oxidized by O2 to form catalytic oxidation reaction of elemental sulfur. On the one hand, the catalyst 5c bed on the left side is protected so that it can be fully cooled and maintained at relatively mild reaction conditions. On the other hand, the protection of the corrugated cooling tube 51 is taken into account, and the catalyst 5c bed on the right side is allowed to fully react exothermically, thereby achieving the technical purpose of targeted control of the reaction conditions of different reaction zones on the left and right sides.

[0111] When most of the acid gas enters the reactor through the gap between the top steam outlet mains, the catalyst 5c bed on the right side can be cooled down to a large extent by increasing the flow rate of boiler water in the upper water supply pipe on the right side, while controlling and maintaining the minimum flow rate in the upper water supply pipe on the left side of the reactor to avoid heat damage to the corrugated cooling pipe 51. Combined with the heat transfer in the entire reaction bed, the bed temperature can be controlled to be ≤300°C, and the H2S in different reaction areas can be directly oxidized by O2 to catalytic oxidation reaction of elemental sulfur. On the one hand, the catalyst 5c bed on the right side is protected so that it is fully cooled and maintained at relatively mild reaction conditions. On the other hand, the protection of the corrugated cooling pipe 51 is taken into account, and the catalyst 5c bed on the left side is fully exothermic. This can achieve the technical purpose of targeted control of reaction conditions in different reaction areas on the left and right sides.

[0112] By setting a water flow regulating valve on the independent upper water pipe corresponding to the corrugated cooling pipe 51 after the partition is grouped, the above-mentioned regional control can be formed, and further the control and adjustment of the reaction conditions in different reaction areas can be realized, achieving the technical effect of controllable heat transfer and controlling the temperature of the reaction zone, and at the same time, the overall coordinated and balanced operation of the catalyst 5c inside the reactor can be achieved, thereby extending the long-term service life of the catalyst 5c.

[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 pointed out that the steam drum 11 in the present application is a pressurized device. The steam pressure generated in the steam drum 11 provides the delivery pressure for the boiler feed water. At the same time, the pressure of the by-product steam in the cooling pipe in the reactor is greater than the pressure in the steam drum 11, so the relative flow of water and steam can be maintained.

[0118] At the same time, the steam drum 11 is connected to a boiler water delivery pipe 52, which is mainly used to introduce boiler water into the steam drum 11 and allow the boiler water to enter the cooling pipe in the reactor through the water delivery pipe. In order to achieve the controllable heat transfer angle, the boiler water flow regulating valve 52c arranged on the boiler water delivery pipe 52 is also controlled and adjusted.

[0119] Specifically, during the reaction process, the external replenishment of boiler water and the external delivery of steam are continuous dynamic processes. The dynamic replenishment flow of the drum 11 can be controlled by the boiler water flow regulating valve 52c, and the external steam production of the drum 11 can be controlled by adjusting the angle of the liquid level of the drum 11. Therefore, from this perspective, the flow regulation of boiler water can also indirectly play a role in regulating the temperature of the reaction zone, and then combined with the boiler water flow entering the cooling pipe, 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 processing volume of the acid gas fluctuates and cannot be actually controlled, the heat release and temperature in the upper reaction zone 5a cannot be accurately predicted. In order to control the reaction temperature of the upper reaction zone 5a and remove the reaction heat in time, the amount of boiler water introduced into the upper reaction zone 5a through the water flow regulating valve of the steam drum 11 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 boiler water introduced into the upper reaction zone 5a through the water flow regulating valve can achieve the basic purpose of controllable heat removal. In other words, no matter how the supply amount changes dynamically, there is a most concerned basis, which is to follow the fluctuation of the acid gas flow or the uncertain reaction rate of the catalytic oxidation catalyst 5c to maintain the controllable reaction temperature of 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 connected to the water inlet short pipe interface through the partitioned water inlet branch pipes.

[0126] The inner ring water inlet branch pipe 501 corresponding to the inner ring corrugated cooling pipe 511 and the middle ring water inlet branch pipe 502 corresponding to the middle ring corrugated cooling pipe 512 are connected through the inner water inlet connecting pipe, so that the inner ring water inlet branch pipe 501 and the middle ring water inlet branch pipe 502 are connected in the lumen, forming the water delivery lumen of the inner ring and middle ring cooling pipes. Furthermore, the outer ring water inlet branch pipe 503 corresponding to the outer ring corrugated cooling pipe 513 and the middle ring water inlet branch pipe 502 corresponding to the middle ring corrugated cooling pipe 512 are connected through the outer water inlet connecting pipe, so that the middle ring water inlet branch pipe 502 and the outer ring water inlet branch pipe 503 are connected in the lumen, forming the water delivery lumen of the outer ring and middle ring cooling pipes. A first water inlet short pipe interface 506 and a second water inlet short pipe interface 507 are provided on both sides of the outer ring water inlet branch pipe 503, which are respectively connected to the two blocking partitioned pipe sections on the outer ring water inlet branch pipe 503 to maintain the water supply relationship for the corrugated cooling pipes 51 after the partitions are grouped.

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

[0128] Similarly, from the perspective of steam output, the steam outlet main pipe includes a plurality of steam outlet branch pipes that are arranged in a ring and interconnected with each other, including 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 on the steam outlet branch pipes to isolate different steam outlet branch pipes. That is to say, two blocking blocks 500 are arranged on 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, which separate 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 sections. In order to enable the steam outlet branch pipes at different positions to export steam from the corresponding corrugated cooling pipe 51, the steam outlet branch pipes in each partition are connected through the steam outlet connecting pipe, and the steam outlet connecting pipe is connected to the steam outlet branch pipe 51. The connecting pipe is arranged in the same radial direction of the steam outlet branch pipe, so that the steam outlet branch pipes after partition blocking can be connected. Furthermore, the steam outlet connecting pipe includes 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, so as to realize 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 connected to the steam outlet short pipe interface through the steam outlet branch pipe isolated by the partition.

[0131] The inner ring steam outlet branch pipe 521 corresponding to the inner ring corrugated cooling pipe 511 and the middle ring steam outlet branch pipe 522 corresponding to the middle ring corrugated cooling pipe 512 are connected through the inner steam outlet connecting pipe, so that the pipe cavities of the inner ring steam outlet branch pipe 521 and the middle ring steam outlet branch pipe 522 are connected, forming the steam transmission pipe cavities of the inner ring and middle ring cooling pipes.

[0132] Furthermore, the outer ring steam outlet branch pipe 523 corresponding to the outer ring corrugated cooling pipe 513 and the middle ring steam outlet branch pipe 522 corresponding to the middle ring corrugated cooling pipe 512 are connected through the outer steam outlet connecting pipe, so that the tube cavity of the middle ring steam outlet branch pipe 522 and the outer ring steam outlet branch pipe 523 are connected, forming the steam transmission tube 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, which are respectively connected to the two blocking partitioned pipe sections on the outer ring steam outlet branch pipe 523, so as to maintain the steam outlet relationship of the corrugated cooling pipe 51 after the partitions are grouped.

[0133] The upper steam pipeline includes a first upper steam pipeline 524 and a second upper steam pipeline 525. The steam outputs of the first upper steam pipeline 524 and the second upper steam pipeline 525 are collected in the steam drum 11. The first steam outlet short pipe interface 526 is connected to the first upper steam pipeline 524, and the second steam outlet short pipe interface 527 is connected to the second upper steam pipeline 525, so that by-product steam can be output to the steam drum 11 at the same time.

[0134] By disposing a first water flow regulating valve 52a on the first upper water supply pipe 504 and a second water flow regulating valve 52b on the second upper water supply pipe 505, the technical objectives of simultaneously inletting water and specifically controlling the inlet water volume can be achieved.

[0135] It should be noted that the specific number of rings of the corrugated cooling tube 51 is not limited in the present application. It can be understood that when there are more rings of corrugated heat exchange tubes, the water inlet branch pipes or steam outlet branch pipes corresponding to the multi-ring corrugated cooling tubes 51 can be spatially connected and aggregated, and an external water supply pipeline or steam supply pipeline can be connected to the steam drum 11. In combination with setting a regulating valve on the water supply pipeline, a targeted controllable heat transfer effect can also be achieved.

[0136] This application does not limit the number of pipe sections that can be blocked by partitions in the water inlet main pipe or steam outlet main pipe. Figure 4 ,Apart from Figure 3 The water inlet main pipe, steam outlet main pipe and corrugated cooling pipe 51 are divided into two groups on the left and right by the blocking block 500, and can also be divided into four groups in the circumferential direction, and the temperature of different areas can be controlled by adjusting the water supply through the independent upper water supply pipeline corresponding to each group.

[0137] In order to ensure a sufficient catalytic oxidation reaction effect, after the reaction in the main reaction area of ​​the upper reaction zone 5a, the remaining H2S in the acid gas continues to undergo oxidation reaction in the lower reaction zone 5b of the catalytic oxidation reactor 5. During the reaction, boiler water is introduced into the cooling pipe in the lower reaction zone 5b to cool the reaction bed, and the bed temperature is controlled to be ≤300°C, so that the H2S in the acid gas that has not been completely reacted in the upper reaction zone 5a 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. A plurality of straight cooling pipes 53 are vertically connected through the catalyst 5c. The number of the straight cooling pipes 53 is determined according to the amount and composition of the acidic gas. Since the degree of catalytic oxidation reaction in the lower reaction zone 5b is lower than that in the upper reaction zone 5a, the cooling pipe of the lower reaction zone 5b is not configured as a corrugated pipe but a straight pipe. The corrugated pipe has wave crests and wave troughs and a larger surface area, which can increase the contact area with the catalytic oxidation catalyst 5c, thereby fully ensuring the cooling effect.

[0139] The cooling effect of the straight tube form is relatively weaker than that of the corrugated tube form, but it is more commonly used and has low cost. Through this setting method, the manufacturing cost of the overall equipment can be reduced based on the reaction degree of different reaction zones, while also ensuring the basic cooling effect on the reaction bed.

[0140] A plurality of straight cooling pipes 53 are arranged in an annular manner around the axial direction of 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] The steam manifold 54 and the boiler water manifold 55 are both arranged in the center of the reactor. Furthermore, the top and bottom ends of the straight tube cooling pipe 53 located in the middle can be directly connected to the steam manifold 54 and the water manifold, and the straight tube cooling pipe 53 outside the steam manifold 54 and the water manifold is connected to the steam manifold 54 and the water manifold through the bends located on both sides of the top and bottom, which can increase the number of pipes and ensure the cooling effect, while offsetting the defect that the cooling effect is weaker than that of the corrugated tube.

[0142] The steam header 54 is connected to a lower steam outlet main pipe 56, the pipe mouth of which extends out of the reactor and is connected to the drum 11 through a lower steam delivery pipeline 57, and the boiler water header 55 is connected to a lower water inlet main pipe 58, which extends out of the reactor and is connected to the drum 11 through a lower water delivery pipeline 59. With this arrangement, normal water delivery and normal steam delivery to the lower reaction zone 5b can be ensured, and the phase change of the lower inlet water is also converted, and the reaction bed is cooled by using the phase change latent heat of the boiler water, and the by-product steam is delivered to the drum 11.

[0143] By means of the sulfur recovery controllable heat transfer reaction device of the present invention, the reaction temperature of different beds inside the catalytic oxidation reactor 5 can be controlled to the greatest extent, while achieving a good desulfurization effect.

[0144] Based on the process flow described above, the present invention also provides a controllable heat transfer sulfur recovery system, including a reaction unit and a sulfur recovery unit, wherein 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-mentioned sulfur recovery controllable heat transfer reaction device and a connecting pipeline;

[0145] The sulfur yield increasing unit, as another core technical point, includes a medium-temperature condenser 6, a sulfur separator 7, a low-temperature condenser 8, an adsorption reaction device 9, an exhaust gas detector 10 and connecting pipes.

[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 by 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 acid gas preheater 3, an air intake pipeline 23 is connected to the cold side of the first acid gas preheater 1, and the cold side outlet branch pipelines of the third acid gas preheater 4 are respectively connected to the downstream adsorption reaction device 9 for providing regenerated acid gas in the regeneration process.

[0148] The first acid gas preheater 1 uses the waste heat of the reaction tail gas to heat the acid gas transported through the air inlet pipe 23. After the acid 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 acid gas, and uses a room temperature organic sulfur hydrolysis catalyst 5c. A small amount of steam is introduced into the hydrolysis reactor 2, so that the organic sulfur and other sulfides in the acid gas react with the trace steam under the catalytic action of the catalyst 5c, and are hydrolyzed to generate H2S that is easy to remove. The reaction is:

[0149] COS+H2O→H2S+CO2

[0150] CS2+2H2O→2H2S+CO2

[0151] The acid gas after hydrolysis is mixed with an appropriate amount of air and enters the second acid gas preheater 3. The third acid gas preheater 4 is heated to 200°C by the waste heat of the reaction tail gas and steam preheating. Part of the heated acid 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 is composed of a shell, a head and an internal water-cooling tube. The catalytic oxidation catalyst 5c is filled between the water-cooling tubes. The catalyst 5c is supported by an inert porcelain ball. 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 heat release. 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 gas production scale of the acid gas of the established device. The number and size of the corrugated cooling tubes 51A1-An of the upper reaction zone 5a and the straight tube cooling tubes 53 B1-Bn of the lower reaction zone 5b are determined by the reaction rate and the heat release.

[0153] Through the above-mentioned configuration, during the design and processing stage of the catalytic oxidation reactor 5, the catalyst 5c loading range and the heat transfer range can be adaptively adjusted for a device of a specific scale.

[0154] Regarding the connection between the two system units, the outlet of the catalytic oxidation reactor 5 is connected to the hot side of the second acid gas preheater 3 to recover part of the heat of the mixed gas, the hot side outlet of the second acid gas preheater 3 is connected to the hot side of the first acid gas preheater 1 to continue to recover the remaining heat, and the hot side outlet of the first acid gas preheater 1 is connected to the sulfur recovery 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 acid gas flow rate. From another perspective, the upper adsorption zone and the lower reaction zone can be set according to the acid gas production scale of a given device to determine the loading amounts of the adsorbent 9c and the Claus catalyst 9d.

[0165] The upper adsorption zone is filled with 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 Claus catalyst 9d, and the acid gas containing H2S transported from the cold side outlet of the upstream third acid gas preheater 4 desorbs H2S and SO2 in the adsorbent 9c, and at the same time, the Claus reaction is carried out in the lower reaction zone to convert it into elemental sulfur and then circulate back to the inlet pipe of the catalytic oxidation reactor 5. The adsorbent 9c and the Claus catalyst 9d are both supported by inert porcelain balls.

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

[0167] The tail gas from the hot side of the low-temperature condenser 8 is passed into the adsorption reactor to adsorb the remaining H2S and SO2. When the adsorption reactor reaches saturation with the adsorption of H2S and SO2, it is switched to another adsorption reactor, and the acid gas from the cold side outlet of the third acid gas preheater 4 is used to reduce and regenerate this reactor. The two adsorption reactors are switched cyclically.

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

[0169] In view of the fact that one adsorption reactor and one regeneration reactor are running simultaneously, the outlets of the two adsorption reactors are respectively connected to the ventilation main pipes for outputting clean gas, which are used for detecting and discharging the gas through the exhaust gas detector 10, and for circulating and returning the output to purge and cool the regenerated adsorption reactor with the clean gas.

[0170] The two adsorption reactors are respectively connected to the ventilation main pipe for exporting the purge gas, so as to circulate the sulfur vapor and the purge gas generated by the Claus reaction during the regeneration process back to the inlet pipe of the catalytic oxidation reactor 5.

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

[0172] The regenerated acid 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℃-400℃, which can promote the Claus reaction and maximize the regeneration of SO2. The reaction is:

[0173] 2H2S+SO2→3S+2H2O

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

[0175] Specifically, the air outlet pipeline valve group includes a first air outlet pipeline valve group 91 and a second air outlet pipeline valve group 92; the first air outlet pipeline valve group 91 is used to output clean gas, the exhaust gas detector 10 is connected to the clean gas external exhaust pipe 15 connected to the ventilation main pipe of the first air outlet pipeline valve group 91, and the clean gas external exhaust pipe 15 upstream of the exhaust gas detector 10 is connected to a clean gas inlet pipe 16, and the clean gas inlet pipe 16 is connected to a clean gas induced draft fan 17, and the clean gas induced draft fan 17 is connected to the ventilation main pipe of one group of the air inlet pipeline valve groups through a clean gas supply pipe 18, and the pipeline valve group includes a seventh control valve V7 and an eighth control valve V8, which correspond to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

[0176] The second gas outlet pipeline valve group 92 is used for internal circulation to export the purge gas during regeneration and purge processes. The root of the purge gas pipeline 12 is connected to the ventilation main pipe of the second gas outlet pipeline valve group 92. The pipeline valve group includes a ninth control valve V9 and a tenth control valve V10, which correspond to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

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

[0178] The first air inlet pipeline valve group 93 is used to introduce regenerated acid gas. The ventilation main pipe is connected to the cold side of the third acid gas preheater 4 through a pipeline. The pipeline valve group includes a first control valve V1 and a second control valve V2, which correspond to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

[0179] The second air inlet pipeline valve group 94 is used to introduce the exhaust gas after sulfur separation, and is used to adsorb H2S and SO2 in the exhaust gas. The ventilation main pipe is connected to the hot side of the low-temperature condenser 8 through a pipeline. The pipeline valve group includes a third control valve V3 and a fourth control valve V4, which correspond to the first adsorption reactor 9a and the second adsorption reactor 9b respectively.

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

[0181] In the specific operation process, combined with Figure 1 , to illustrate with a specific example:

[0182] The tail gas from the low-temperature condenser 8 first enters the first adsorption reactor 9a to adsorb residual H2S and SO2. At this time, the third control valve V3 and the seventh control valve V7 are opened, and 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, so that the first adsorption reactor 9a is adsorbed and the second adsorption reactor 9b is regenerated.

[0183] The exhaust gas at the outlet of the first adsorption reactor 9a is detected online by the exhaust gas detector 10, and the H2S concentration reaches 0.03 mg / Nm 3 Or SO2 concentration reaches 10mg / Nm 3 When switching to the second adsorption reactor 9b for adsorption, the control valves second control valve V2, third control valve V3, sixth control valve V6, seventh control valve V7 and tenth control valve V10 are closed, and the control valves fourth control valve V4 and eighth control valve V8 are opened, so that the second adsorption reactor 9b is adsorbed and the first adsorption reactor 9a is regenerated.

[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 and cooled to wait 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 SO2 concentration reaches 10mg / Nm 3When switching to the first adsorption reactor 9a adsorption process, the second adsorption reactor 9b enters the regeneration process, and the switching is repeated in sequence. Through the setting of the above control valve, the switching between adsorption and regeneration can be performed to ensure the stability and reliability of normal tail gas adsorption and desorption regeneration.

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

[0187] The acid gas is heated to 70°C by the first acid gas preheater 1 and then enters the hydrolysis reactor 2. The catalyst 5c of the hydrolysis reactor 2 is loaded with 20m³. Under the catalytic action of the catalyst 5c, organic sulfur such as COS in the mixed gas reacts with a trace amount of water vapor and hydrolyzes to generate H2S which is easy to remove. Then, it is mixed with 7150Nm³ / h of air and enters the second acid gas preheater 3 and the third acid gas preheater 4, where it is preheated to 200°C by the reaction gas and steam in turn. Part of the mixed gas enters the catalytic oxidation reactor 5 from the top, and the other part is used for regeneration of the adsorption reactor of the sulfur recovery 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 loaded with a catalytic oxidation catalyst 5c with a loading volume of 20m³. The inlet of the corrugated cooling pipe 51 is connected to the water inlet main pipe arranged along the reactor ring, and the outlet of the corrugated cooling pipe 51 is connected to the steam outlet main pipe arranged along the reactor ring. Under the action of the catalyst 5c, H2S reacts with oxygen to generate elemental sulfur and produce trace amounts of SO2. The temperature is reduced by the corrugated cooling pipe 51 arranged in the upper reaction zone 5a, and the temperature of the reaction zone is controlled to be ≤300℃. The by-product steam is 6.2t / h, and the steam enters the steam drum 11. The remaining unreacted acid gas enters the lower reaction zone 5b.

[0189] The lower reaction zone 5b is filled with catalytic oxidation catalyst 5c, with a filling volume of 30m³, and a straight tube cooling pipe 53 is provided. The upper end of the straight tube cooling pipe 53 is connected to the centrally arranged steam header 54, and is collected to the steam outlet main pipe, and the lower end is connected to the centrally arranged boiler water header 55, and is collected to 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 trace SO2. The temperature is reduced by the straight tube cooling pipe 53 arranged in the lower reaction zone 5b, and the reaction zone temperature is controlled to be ≤300℃. The by-product steam is 3.4t / h, and the steam enters the steam drum 11. The H2S concentration in the outlet mixed gas of the catalytic oxidation reactor 5 is less than 0.01%, and the SO2 concentration is less than 0.1%.

[0190] The mixed gas enters the second acid gas preheater 3 to recover part of the heat, then enters the first acid gas preheater 1 to recover the remaining heat, and finally enters the medium-temperature condenser 6 to recover the remaining heat, and the temperature drops to 150°C. The cooled mixed gas enters the sulfur separator 7, and passes through the internal defoaming net. The liquid sulfur mist entrained in the mixed gas in the sulfur separator 7 is separated in the defoaming net. 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 to sulfur molding. The sulfur recovery is 4291kg / 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 recovery unit. The SO2 emission concentration in the clean gas after treatment by the sulfur recovery unit is lower than 10mg / Nm 3 , H2S emission concentration is less than 0.03mg / Nm 3 .

[0191] Through the sulfur recovery controllable heat transfer reaction device and sulfur recovery system in the present application, it is possible to effectively desulfurize low-concentration H2S acid gas, and can be suitable for the treatment of acid gas with an H2S concentration of 1%-15% in the form of controllable heat transfer. By adjusting the reaction temperature, it is possible to achieve the treatment of acid gas with different H2S contents within a low concentration range, and to achieve increased sulfur recovery.

[0192] It should be noted that, in the absence of conflict, the features in the embodiments of this application may be combined with each other.

[0193] The above description is only the preferred embodiment of the present application and is not intended to limit the present application. For those skilled in the art, the present application may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included in the protection scope of the present 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 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 is 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 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 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 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 cold side of the medium-temperature condenser is connected to a medium-temperature boiler water pipeline, and the produced steam is passed through a medium-temperature steam pipeline into a steam outlet main pipe connected to the steam drum; The adsorption reaction device is connected to the air inlet pipeline of the catalytic oxidation reactor through a purge gas pipeline, a purge gas induced draft fan and a purge gas delivery pipeline which are connected in sequence.

8. The controllable heat transfer sulfur recovery system according to claim 7, characterized in that: The adsorption reaction device comprises a first adsorption reactor and a second adsorption reactor 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 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 the clean air discharge pipeline connected to the ventilation main pipe of the first air outlet pipeline valve group, and the clean air discharge pipeline upstream of the exhaust gas detector is connected to a clean air bleed pipeline, 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 the 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 first adsorption reactor and the second adsorption reactor 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; The upper adsorption zone is filled with an adsorbent, and the lower reaction zone is filled with a Claus catalyst. Both the adsorbent and the Claus catalyst are supported by inert ceramic balls.

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