A coke oven gas fine desulfurization system

Abstract

The utility model provides a coke oven gas fine desulfurization system, including the gas pressurization unit, pretreatment unit, waste heat recovery unit, organic sulfur conversion unit, gas heater, gas cooler, hydrogen sulfide adsorption unit and hydrogen sulfide regeneration branch that connect gradually. The gas pressurization unit pressurizes to 5-30kPa with coke oven gas;Pretreatment unit adopts and sets up multiple pretreatment towers in parallel, and is loaded with activated carbon and coke composition;Organic sulfur conversion unit contains and fills in the hydrolysis catalyst and is connected with waste heat recovery unit in parallel organic sulfur conversion tower;Hydrogen sulfide adsorption unit is equipped with multiple parallel adsorption towers, and is loaded with supported carbon-based desulfurization catalyst;Hydrogen sulfide regeneration branch sends desorption gas to sulfur making equipment. The system realizes the efficient removal of sulfide in coke oven gas through the cooperation of multiple units, optimizes the thermal energy utilization efficiency, and improves the stability of system operation.

Description

Technical Field

[0001] This utility model relates to the field of coke oven gas desulfurization technology, specifically to a coke oven gas fine desulfurization system. Background Technology

[0002] Coke oven gas, a significant byproduct of the steel and coking industries, requires purification as a crucial step for resource utilization. The sulfides in the gas primarily consist of inorganic and organic sulfur, which not only corrode pipelines and equipment but also poison subsequent chemical catalysts. Therefore, fine desulfurization processes are paramount. Traditional desulfurization systems typically employ multi-stage series fixed-bed reactors, converting organic sulfur through catalyst hydrolysis followed by hydrogen sulfide removal using adsorbents. However, in actual industrial production, coke oven gas is characterized by large pressure fluctuations and complex composition, posing a significant challenge to the stable operation of desulfurization systems. Currently, desulfurization processes often suffer from unstable desulfurization efficiency, high energy consumption, and insufficient system synergy, particularly when dealing with fluctuating gas parameters, making it difficult to balance desulfurization accuracy with operational economy. Therefore, constructing a highly adaptable and energy-optimized efficient desulfurization system has become a pressing technical challenge for the industry. Utility Model Content

[0003] In view of the above problems, this utility model provides a coke oven gas fine desulfurization system, which realizes efficient and stable removal of sulfides under low pressure conditions, and solves the problems of low desulfurization efficiency and high energy consumption of traditional systems.

[0004] To achieve the above objectives, this application provides a coke oven gas desulfurization system, comprising: a gas pressurization unit, a pretreatment unit, a waste heat recovery unit, an organic sulfur conversion unit, a gas heater, a gas cooler, a hydrogen sulfide adsorption unit, and a hydrogen sulfide regeneration branch. The gas pressurization unit is connected to the inlet pipeline and is used to pressurize the coke oven gas to 5-30 kPa. The pretreatment unit is connected to the output end of the gas pressurization unit and includes multiple pretreatment towers arranged in parallel. Each pretreatment tower is filled with a combination of activated carbon and coke, and each pretreatment tower has a programmable valve group at its inlet and outlet. The waste heat recovery unit is connected to the pretreatment unit. The organic sulfur conversion unit is connected to the pretreatment unit and also to the waste heat recovery unit. The organic sulfur conversion unit includes at least two organic sulfur conversion towers connected in parallel, each filled with a hydrolysis catalyst. A gas heater is connected to the organic sulfur conversion unit. A gas cooler is connected to the output end of the organic sulfur conversion unit. A hydrogen sulfide adsorption unit is connected to the output end of the gas cooler. The hydrogen sulfide adsorption unit includes multiple hydrogen sulfide adsorption towers connected in parallel, each filled with a supported carbon-based desulfurization catalyst. A hydrogen sulfide regeneration branch is connected between the hydrogen sulfide adsorption unit and the sulfur production equipment to send the desorbed gas from the adsorption towers to the sulfur production equipment.

[0005] In some embodiments, the gas pressurization unit is configured as a centrifugal fan or a Roots blower; the number of gas pressurization units is two or three; when the number of gas pressurization units is two, the two gas pressurization units are configured in a one-in-one-standby mode; when the number of gas pressurization units is three, the three gas pressurization units are configured in a two-in-one-standby mode.

[0006] In some embodiments, the program-controlled valve assembly includes at least one of a pneumatic shut-off valve, an electric regulating valve, a pressure sensor, and a control unit.

[0007] In some embodiments, the pneumatic shut-off valve and the electric regulating valve are arranged in parallel; the control unit is electrically connected to the pneumatic shut-off valve, the electric regulating valve, and the pressure sensor, respectively.

[0008] In some embodiments, the porosity of the activated carbon and coke composition is configured to be 40% to 65%.

[0009] In some embodiments, the waste heat recovery unit is configured as a tubular heat exchanger or a plate heat exchanger.

[0010] In some embodiments, the hydrogen sulfide regeneration branch further includes: a desorption pressurizing blower and a desorption gas heater, wherein the desorption pressurizing blower is connected to the hydrogen sulfide adsorption unit; and the desorption gas heater is connected to the output end of the desorption pressurizing blower for heating the desorbed gas.

[0011] In some embodiments, the coke oven gas desulfurization system further includes a pretreatment regeneration branch, which is connected between the pretreatment unit and the gas pressurization unit, for sending the desorbed gas from the pretreatment tower back to the gas pressurization unit.

[0012] In some embodiments, the hydrogen sulfide adsorption unit further includes: a tower pressure balancing pipeline and a differential pressure detector, wherein the tower pressure balancing pipeline is connected to the top of each hydrogen sulfide adsorption tower arranged in parallel; and the differential pressure detector is respectively installed on the inlet and outlet pipelines of each hydrogen sulfide adsorption tower.

[0013] In some embodiments, the waste heat recovery unit includes: a plurality of heat exchanger modules arranged in parallel, a switching valve group and a backflush pipeline. The switching valve group includes a plurality of switching valves, each of which is respectively located at the connection end of each heat exchanger module and is used to control the operating status of each heat exchanger module. The backflush pipeline is connected between the outlet of the gas pressurization unit and the heat exchanger module.

[0014] Unlike existing technologies, the above-mentioned technical solution provides a coke oven gas desulfurization system, comprising a gas pressurization unit, a pretreatment unit, a waste heat recovery unit, an organic sulfur conversion unit, a gas heater, a gas cooler, a hydrogen sulfide adsorption unit, and a hydrogen sulfide regeneration branch connected in sequence. The gas pressurization unit pressurizes the coke oven gas to 5-30 kPa; the pretreatment unit uses multiple pretreatment towers connected in parallel, filled with a combination of activated carbon and coke; the organic sulfur conversion unit includes parallel organic sulfur conversion towers, filled with a hydrolysis catalyst and connected to the waste heat recovery unit; the hydrogen sulfide adsorption unit has multiple parallel adsorption towers, filled with a supported carbon-based desulfurization catalyst; the hydrogen sulfide regeneration branch sends the desorbed gas to sulfur production equipment. This system, through the coordinated operation of multiple units, achieves efficient removal of sulfides from coke oven gas, while optimizing thermal energy utilization efficiency and improving system operational stability.

[0015] The above description of the utility model is merely an overview of the technical solution of this utility model. In order to enable those skilled in the art to better understand the technical solution of this utility model and to implement it based on the description and drawings, and to make the above-mentioned objectives and other objectives, features and advantages of this utility model easier to understand, the following description is provided in conjunction with the specific embodiments and drawings of this utility model. Attached Figure Description

[0016] The accompanying drawings are only used to illustrate the principles, implementation methods, applications, features, and effects of the present invention and other related contents, and should not be considered as limitations on the present invention.

[0017] In the accompanying drawings of the instruction manual:

[0018] Figure 1 This is a schematic diagram of the specific structure of the coke oven gas desulfurization system described in the specific implementation method;

[0019] Figure 2 This is a schematic diagram of the specific structure of the preprocessing unit described in the specific implementation method;

[0020] Figure 3 This is a schematic diagram of the specific structure of the organic sulfur conversion unit described in the specific embodiment;

[0021] Figure 4 This is a schematic diagram of the specific structure of the hydrogen sulfide regeneration branch described in the specific implementation method;

[0022] Figure 5 This is a schematic diagram of the specific structure of the waste heat recovery unit described in a specific implementation.

[0023] The reference numerals used in the above figures are explained as follows:

[0024] 1. Gas pressurization unit;

[0025] 2. Preprocessing unit;

[0026] 21. Pretreatment tower;

[0027] 22. Program-controlled valve assembly;

[0028] 3. Waste heat recovery unit;

[0029] 31. Heat exchanger module;

[0030] 32. Switch valve groups;

[0031] 33. Backflush piping;

[0032] 4. Organic sulfur conversion unit;

[0033] 41. Organic sulfur conversion tower;

[0034] 5. Gas heater;

[0035] 6. Gas cooler;

[0036] 7. Hydrogen sulfide adsorption unit;

[0037] 71. Hydrogen sulfide adsorption tower;

[0038] 8. Hydrogen sulfide regeneration branch;

[0039] 81. Desorption and pressurization fan;

[0040] 82. Desorption gas heater;

[0041] 9. Pre-treatment regeneration branch. Detailed Implementation

[0042] To illustrate in detail the possible application scenarios, technical principles, implementable specific solutions, and achievable objectives and effects of this utility model, the following description, in conjunction with the listed specific embodiments and accompanying drawings, provides a detailed explanation. The embodiments described herein are merely illustrative of the technical solutions of this utility model and are therefore intended to limit the scope of protection of this utility model.

[0043] In this document, the term "embodiment" means that a specific feature, structure, or characteristic described in connection with an embodiment may be included in at least one embodiment of this utility model. The term "embodiment" appearing in various places throughout the specification does not necessarily refer to the same embodiment, nor does it specifically limit its independence or connection with other embodiments. In principle, in this utility model, as long as there are no technical contradictions or conflicts, the technical features mentioned in each embodiment can be combined in any way to form corresponding implementable technical solutions.

[0044] Unless otherwise defined, the technical terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains; the use of related terms herein is merely for the purpose of describing particular embodiments and is not intended to limit the invention.

[0045] In the description of this utility model, the term "and / or" is used to describe the logical relationship between objects, indicating that three relationships can exist. For example, A and / or B means: A exists, B exists, and A and B exist simultaneously. Additionally, the character " / " generally indicates that the preceding and following objects have an "or" logical relationship.

[0046] In this invention, terms such as "first" and "second" are used only to distinguish one entity or operation from another, and do not necessarily require or imply any actual quantity, hierarchy, or order between these entities or operations.

[0047] Without further limitations, the use of terms such as “comprising,” “including,” “having,” or other similar expressions in this invention is intended to cover non-exclusive inclusion, which does not exclude the presence of additional elements in a process, method, or product that includes the stated elements, such that a process, method, or product that includes a series of elements may include not only those defined elements but also other elements not expressly listed, or elements inherent to such a process, method, or product.

[0048] Similar to the understanding in the Examination Guidelines, in this utility model, expressions such as "greater than," "less than," and "exceeding" are understood to exclude the stated number; expressions such as "above," "below," and "within" are understood to include the stated number. Furthermore, in the description of the embodiments of this utility model, "multiple" means two or more (including two), and similar expressions related to "multiple" are also understood in this way, such as "multiple groups" and "multiple times," unless otherwise explicitly specified.

[0049] In the description of the embodiments of this utility model, the space-related expressions used, such as "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "vertical," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential," indicate the orientation or positional relationship based on the orientation or positional relationship shown in the specific embodiments or drawings. They are only for the convenience of describing the specific embodiments of this utility model or for the reader's understanding, and do not indicate or imply that the device or component referred to must have a specific position, a specific orientation, or be constructed or operated in a specific orientation. Therefore, they should not be construed as limitations on the embodiments of this utility model.

[0050] Unless otherwise expressly specified or limited, the terms "installation," "connection," "linking," "fixing," and "setting," as used in the description of the embodiments of this utility model, should be interpreted broadly. For example, "connection" can be a fixed connection, a detachable connection, or an integral setting; it can be a mechanical connection, an electrical connection, or a communication connection; it can be a direct connection or an indirect connection through an intermediate medium; it can be the internal connection of two components or the interaction between two components. For those skilled in the art to which this utility model pertains, the specific meaning of the above terms in the embodiments of this utility model can be understood according to the specific circumstances.

[0051] Please see Figures 1 to 5 This embodiment provides a coke oven gas desulfurization system, including: a gas pressurization unit 1, a pretreatment unit 2, a waste heat recovery unit 3, an organic sulfur conversion unit 4, a gas heater 5, a gas cooler 6, a hydrogen sulfide adsorption unit 7, and a hydrogen sulfide regeneration branch 8. The gas pressurization unit 1 is connected to the inlet pipeline and is used to pressurize the coke oven gas to 5-30 kPa. The pretreatment unit 2 is connected to the output end of the gas pressurization unit 1. The pretreatment unit 2 includes multiple pretreatment towers 21 arranged in parallel. Each pretreatment tower 21 is filled with a combination of activated carbon and coke. The inlet and outlet of each pretreatment tower 21 are respectively equipped with a programmable control valve group 22. The waste heat recovery unit 3 is connected to the pretreatment unit 2. Organic sulfur conversion unit 4 is connected to pretreatment unit 2, and organic sulfur conversion unit 4 is also connected to waste heat recovery unit 3. Organic sulfur conversion unit 4 includes at least two organic sulfur conversion towers 41 arranged in parallel, each organic sulfur conversion tower 41 is filled with hydrolysis catalyst; gas heater 5 is connected to organic sulfur conversion unit 4; gas cooler 6 is connected to the output end of organic sulfur conversion unit 4; hydrogen sulfide adsorption unit 7 is connected to the output end of gas cooler 6, hydrogen sulfide adsorption unit 7 includes multiple hydrogen sulfide adsorption towers 71 arranged in parallel, hydrogen sulfide adsorption towers 71 are filled with supported carbon-based desulfurization catalyst; hydrogen sulfide regeneration branch 8 is connected between hydrogen sulfide adsorption unit 7 and sulfur production equipment, used to send the desorbed gas from the adsorption tower to the sulfur production equipment.

[0052] In this embodiment, the gas pressurization unit 1 employs a centrifugal pressurization device to stably pressurize the coke oven gas to 5-30 kPa. Its output is equipped with a pressure feedback regulating valve to adapt to pressure fluctuations at the inlet of the pretreatment unit 2. The pretreatment tower 21 connected in parallel in the pretreatment unit 2 adopts a double-layer packing structure. The lower layer is a coke composition for coarse filtration, and the upper layer is an activated carbon adsorption layer for removing tar and heavy metals. The programmable valve group 22 uses PLC timing control to achieve tower switching and backflushing regeneration. Preferably, the waste heat recovery unit 3 uses a shell-and-tube heat exchanger to exchange heat with the high-temperature outlet gas of the organic sulfur conversion unit 4. The recovered heat energy is used for preheating the inlet gas of the hydrolysis reaction.

[0053] The organic sulfur conversion tower 41 is filled with an aluminum-based hydrolysis catalyst, preferably with a honeycomb structure to increase the contact area. Parallel switching between towers can be achieved via an electrically operated three-way valve. The hydrogen sulfide adsorption tower 71 is filled with a supported carbon-based desulfurization catalyst, which is zinc oxide-modified activated carbon, and its pore structure is adapted to the chemical adsorption requirements of hydrogen sulfide. The hydrogen sulfide regeneration branch 8 is equipped with an electrically heated desorption device; the desorbed gas is condensed and separated before being sent to the sulfur production equipment.

[0054] Coke oven gas flows sequentially through the gas pressurization unit 1 for stabilization before entering the pretreatment unit 2. The parallel pretreatment towers 21 operate continuously and regenerate under program control, effectively intercepting particulate matter and tar. After pretreatment, the gas is heated by the waste heat recovery unit 3 and then enters the organic sulfur conversion unit 4, where organic sulfur is converted to hydrogen sulfide under the action of a catalyst. The recovered waste heat reduces system energy consumption. The converted gas is then cooled and enters the hydrogen sulfide adsorption unit 7. The multi-tower parallel design ensures continuous adsorption, and efficient hydrogen sulfide removal is achieved through a supported catalyst. The saturated hydrogen sulfide adsorption tower 71 desorbs and recovers elemental sulfur through the hydrogen sulfide regeneration branch 8. This system achieves deep sulfide removal under low-pressure conditions through multi-unit coordinated control and energy cascade utilization. The parallel tower structure of the pretreatment tower 21 and the program-controlled valve group 22 significantly improve operational stability. The hydrogen sulfide regeneration branch 8 simultaneously achieves sulfur resource recovery, and the overall process balances processing efficiency and economy.

[0055] In some embodiments, the gas pressurization unit 1 is configured as a centrifugal fan or a Roots blower; the number of gas pressurization units 1 is two or three; when the number of gas pressurization units 1 is two, the two gas pressurization units 1 are configured in a one-in-one-backup mode; when the number of gas pressurization units 1 is three, the three gas pressurization units 1 are configured in a two-in-one-backup mode.

[0056] In this embodiment, the gas pressurization unit 1 is specifically configured as a centrifugal blower or a Roots blower. Centrifugal blowers are suitable for high-flow, low-pressure conditions, while Roots blowers are better suited for high-pressure, low-flow requirements. The number of gas pressurization units 1 is set to two or three. With two units, a one-in-one-backup mode is used, with the backup unit automatically switching in case of a main unit failure. With three units, a two-in-one-backup mode is used, improving gas supply stability through load balancing. Preferably, buffer tanks are installed at the blower inlet and outlet to smooth pressure fluctuations, and the backup unit is equipped with a preheating system to ensure immediate start-up.

[0057] By employing redundant configurations of multiple gas pressurization units 1, the system can continue to supply gas even in the event of a single unit failure. The one-in-one-backup or two-in-one-backup modes significantly improve operational reliability. Buffer tanks reduce the impact of airflow fluctuations on subsequent processes, and the preheating system shortens the response time of the backup units. This embodiment achieves seamless integration of equipment maintenance and system operation while ensuring pressure stability, making it suitable for industrial scenarios in coke oven gas processing where continuous gas supply is critical.

[0058] In some embodiments, the program-controlled valve group 22 includes at least one of a pneumatic shut-off valve, an electric regulating valve, a pressure sensor, and a control unit.

[0059] In this embodiment, a pneumatic shut-off valve is used to quickly shut off the pipeline, and its valve body is preferably made of stainless steel for corrosion resistance; an electric regulating valve continuously adjusts the flow rate by driving the valve core with a motor, adapting to a smooth pressure transition during the switching of pretreatment tower 21; a pressure sensor monitors the pipeline pressure in real time and transmits the signal to the control unit. The control unit is a PLC or DCS system, which coordinates the valve action sequence according to a preset program. Preferably, the valve group is equipped with a manual operating mechanism as an emergency backup, and redundant sensors are set at key nodes to improve reliability.

[0060] The program-controlled valve group 22 achieves rapid shut-off via a pneumatic shut-off valve, while an electrically controlled regulating valve ensures precise flow control. A pressure sensor and control unit form a closed-loop regulation system, guaranteeing stable system pressure during the switching process of the pretreatment tower 21. A manual operating mechanism provides emergency backup, and redundant design reduces the risk of failure. This embodiment enables the pretreatment unit 2 to achieve fully automatic continuous operation and regeneration, significantly improving the stability and ease of operation of the coke oven gas treatment system.

[0061] In some embodiments, the pneumatic shut-off valve and the electric regulating valve are arranged in parallel; the control unit is electrically connected to the pneumatic shut-off valve, the electric regulating valve, and the pressure sensor, respectively.

[0062] In this embodiment, the pneumatic shut-off valve and the electric regulating valve are arranged in parallel. The pneumatic shut-off valve is used for rapid shut-off in emergency situations, and its actuator is driven by compressed air with a response time controlled in milliseconds. The electric regulating valve is used for fine flow regulation under normal operating conditions, and its opening degree is precisely controlled by a servo motor. The parallel arrangement of the two valves can give full play to their respective advantages and avoid functional overlap. The control unit establishes a connection with the pneumatic shut-off valve, the electric regulating valve, and the pressure sensor through hardwiring or fieldbus, and collects pressure data in real time and outputs control commands. Preferably, a check valve is installed on the parallel pipeline of the valves to prevent backflow of the medium from interfering with the regulation accuracy; the control unit is equipped with a dual-channel communication module to ensure the reliability of signal transmission.

[0063] The parallel arrangement of the pneumatic shut-off valve and the electric regulating valve ensures both the safety requirement of rapid system shut-off and the precision requirements of process regulation. The control unit coordinates the actions of the two valves by monitoring pressure changes in real time. In case of emergencies, the pneumatic shut-off valve is triggered first to protect the system, while the electric regulating valve maintains process stability during normal operation. This embodiment improves system response speed and ensures control accuracy, while enhancing overall reliability through redundancy design. It is particularly suitable for operating environments in coke oven gas treatment where both safety and adjustability are critical.

[0064] In some embodiments, the porosity of the activated carbon and coke composition is configured to be 40% to 65%.

[0065] In this embodiment, the porosity of the activated carbon and coke composition is controlled within the range of 40% to 65%, which ensures sufficient adsorption surface area while maintaining appropriate mechanical strength. Preferably, the activated carbon and coke in the composition are mixed in a 3:7 ratio, which utilizes both the high adsorption capacity of the activated carbon and the structural stability of the coke.

[0066] This embodiment sets the porosity of the activated carbon and coke composition in the range of 40% to 65%, so that the composition has both excellent adsorption performance and structural strength, effectively treating impurities in coal gas, while extending its service life.

[0067] In some embodiments, the waste heat recovery unit 3 is configured as a tubular heat exchanger or a plate heat exchanger.

[0068] In this embodiment, the tubular heat exchanger consists of multiple metal tubes forming the heat exchange channel, suitable for high-temperature and high-pressure conditions. Its tube bundle can be made of stainless steel for corrosion resistance. The plate heat exchanger uses corrugated plates stacked to form flow channels, featuring a compact structure and high-efficiency heat transfer characteristics. Preferably, the tubular heat exchanger can be equipped with spiral turbulence enhances the heat transfer effect, while the plate heat exchanger adopts a detachable design for easy maintenance and cleaning. Both types of heat exchangers recover waste heat from the exhaust gas of the pretreatment tower 21 through heat medium circulation. The type of heat exchanger can be flexibly selected according to actual operating conditions.

[0069] Waste heat recovery unit 3 effectively recovers waste heat from process exhaust gas through tubular or plate heat exchangers. Tubular structures are suitable for harsh operating conditions, while plate structures offer higher heat exchange efficiency. This embodiment achieves energy recovery and utilization, ensuring long-term stable system operation and significantly improving the energy utilization efficiency of the entire coke oven gas treatment system.

[0070] In some embodiments, the hydrogen sulfide regeneration branch 8 further includes: a desorption pressurizing blower 81 and a desorption gas heater 82. The desorption pressurizing blower 81 is connected to the hydrogen sulfide adsorption unit 7; the desorption gas heater 82 is connected to the output end of the desorption pressurizing blower 81 and is used to heat the desorbed gas.

[0071] In this embodiment, the desorption pressurizing blower 81 is directly connected to the hydrogen sulfide adsorption unit 7 to provide the airflow power required for the desorption process. Its pressure range is typically controlled between 5-15 kPa to ensure effective desorption. Furthermore, the desorption pressurizing blower 81 uses a corrosion-resistant impeller to handle sulfur-containing media. The desorption gas heater 82 is located at the output end of the desorption pressurizing blower 81, heating the desorption gas to the operating temperature via electric heating or steam heat exchange. This avoids thermal damage to the adsorption material while ensuring effective desorption of hydrogen sulfide. Preferably, the heater adopts a segmented temperature control design, which can automatically adjust the heating power according to the desorption progress. Preferably, the hydrogen sulfide regeneration branch 8 adopts closed-loop control, which can automatically start and stop according to the saturation state of the adsorption unit, minimizing energy consumption while ensuring desulfurization effect.

[0072] To address the regeneration characteristics of supported carbon-based desulfurization catalysts, a desorption pressurizing blower 81 provides a stable airflow for the regeneration process, ensuring complete desorption of hydrogen sulfide from the catalyst. A desorption gas heater 82 precisely controls the temperature to bring the desorption gas to its optimal operating temperature, improving both the desorption efficiency and protecting the adsorption material. This synergistic effect enables efficient regeneration of the hydrogen sulfide adsorption unit 7, allowing the entire desulfurization system to operate continuously and stably. This system is particularly suitable for the removal and resource recovery of high-concentration hydrogen sulfide from coke oven gas.

[0073] In some embodiments, the coke oven gas desulfurization system further includes a pretreatment regeneration branch 9, which is connected between the pretreatment unit 2 and the gas pressurization unit 1, and is used to send the desorbed gas from the pretreatment tower 21 back to the gas pressurization unit 1.

[0074] In this embodiment, the pretreatment regeneration branch 9 can be connected via a flange to the desorption port of the pretreatment tower 21 and the inlet of the gas pressurization unit 1, with its pipe diameter matching the maximum flow rate of the desorbed gas. Preferably, the pipeline integrates an anti-backflow device to prevent backflow of the medium caused by pressure fluctuations in the gas pressurization unit 1. The gas pressurization unit 1 maintains a constant inlet pressure when receiving desorbed gas, and its frequency conversion control system automatically adjusts the rotation speed according to the regeneration stage signal of the pretreatment tower 21. Preferably, the pretreatment regeneration branch 9 is equipped with an online sulfur component analyzer, which automatically switches to the emergency treatment channel when the sulfur capacity of the desorbed gas exceeds the standard.

[0075] In this embodiment, the organic sulfur compounds desorbed in the pretreatment unit 2 are reintroduced into the main process flow through a directional circulating regeneration gas flow. The gas pressurization unit 1 uniformly mixes the sulfur-containing desorbed gas with fresh gas before conveying it to the subsequent desulfurization section for further treatment. The coordinated control of the pretreatment regeneration branch 9 and the gas pressurization unit 1 avoids the loss of sulfur in gaseous form and reduces regeneration energy consumption through pressure energy recovery. By dynamically adjusting the pressurization parameters, the system ensures stable reflux of the desorbed gas under different operating conditions, maintaining optimal sulfur adsorption activity of the adsorbent material. This system is particularly suitable for continuous production scenarios involving the synergistic removal of organic and inorganic sulfur from coke oven gas.

[0076] In some embodiments, the hydrogen sulfide adsorption unit 7 further includes: a tower pressure balancing pipeline and a differential pressure detector, wherein the tower pressure balancing pipeline is connected to the top of each hydrogen sulfide adsorption tower 71 arranged in parallel; and the differential pressure detector is respectively installed on the inlet and outlet pipelines of each hydrogen sulfide adsorption tower 71.

[0077] In this embodiment, the tower pressure balancing pipeline refers to the gas communication pipeline connecting the tops of each parallel hydrogen sulfide adsorption tower 71, used to balance the internal pressure of each tower. Preferably, this pipeline adopts a ring arrangement to shorten the pressure transmission path. The differential pressure detector refers to the differential pressure sensing device installed on the inlet and outlet pipelines of the hydrogen sulfide adsorption tower 71, used to monitor the operating resistance of each tower in real time. Preferably, the detector signal line is connected to the central control system to achieve automatic data acquisition.

[0078] This embodiment maintains pressure balance among the parallel hydrogen sulfide adsorption towers 71 through a tower pressure balancing pipeline. Combined with real-time monitoring of the pressure difference between the inlet and outlet of each tower by a differential pressure detector, the saturation state of the adsorbent can be accurately determined. When the pressure difference of a hydrogen sulfide adsorption tower 71 exceeds a set threshold, the system automatically switches to standby tower operation and initiates the regeneration program. This effectively solves the flow deviation problem caused by uneven pressure in parallel equipment, ensuring that the sulfur capacity utilization rate of each hydrogen sulfide adsorption tower 71 is basically consistent. Simultaneously, through the linkage of pressure difference data and switching control, accurate judgment and timely regeneration of the working status of the supported carbon-based desulfurization catalyst are achieved, significantly improving the operational stability and continuity of the desulfurization system. This is particularly suitable for large-scale coke oven gas purification devices that require uninterrupted gas supply.

[0079] In some embodiments, the waste heat recovery unit 3 includes: a plurality of heat exchanger modules 31 arranged in parallel, a switching valve group 32 and a backflush pipeline 33. The switching valve group 32 includes a plurality of switching valves, each of which is respectively located at the connection end of each heat exchanger module 31 and is used to control the operating status of each heat exchanger module 31. The backflush pipeline 33 is connected between the outlet of the gas pressurization unit 1 and the heat exchanger module 31.

[0080] In this embodiment, the waste heat recovery unit 3 refers to a device group used to recover the sensible heat of coke oven gas. Its multiple heat exchanger modules 31, arranged in parallel, typically adopt a shell-and-tube structure. Each heat exchanger module 31 is an independent heat exchange unit composed of heat exchange tube bundles and a shell, used to achieve heat exchange between high-temperature gas and a cooling medium. The switching valve group 32 refers to a valve combination consisting of multiple switching valves, each of which is located at the connecting end of the heat exchanger module 31, used to control the operation or isolation status of each module. The backflush pipeline 33 refers to a gas delivery pipeline connected between the outlet of the gas pressurization unit 1 and the heat exchanger module 31, used to purge the shut-down heat exchanger module 31 with pressurized gas. Preferably, the switching valves are pneumatic quick-opening valves to shorten the switching time, and the backflush pipeline 33 is equipped with a flow regulating valve to precisely control the purging intensity.

[0081] This embodiment achieves rapid switching of heat exchanger modules 31 through switching valve group 32. When a heat exchanger module 31 requires maintenance or cleaning, it can be isolated and pressurized gas can be introduced through backflushing pipe 33 for reverse purging. This ensures continuous operation of the waste heat recovery system while effectively removing ash accumulation on the surface of the heat exchanger tube bundle. During the switching process, the gas flow direction remains unchanged, and system pressure fluctuations are controlled within the allowable range, ensuring stable operation of downstream processes. Through modular design and rapid switching function, the operational flexibility and maintenance convenience of the waste heat recovery system are significantly improved. At the same time, the backflushing cleaning mechanism maintains the high-efficiency heat transfer performance of the heat exchanger, making it particularly suitable for waste heat recovery applications of coke oven gas with high dust content.

[0082] By adopting the above technical solutions, this utility model differs from existing technologies and possesses the following beneficial effects: It achieves efficient and stable operation of the coke oven gas desulfurization system through multi-level collaborative control and modular design. The pretreatment unit 2 employs a parallel tower structure and program-controlled valve group 22, ensuring stable removal efficiency of the activated carbon and coke composition during continuous adsorption and regeneration. The organic sulfur conversion unit 4 achieves efficient conversion of organic sulfur through a parallel hydrolysis catalyst tower, and the energy cascade utilization of the waste heat recovery unit 3 significantly reduces system energy consumption. The hydrogen sulfide adsorption unit 7 adopts a combined design of parallel tower pressure balance pipelines and differential pressure detectors, ensuring balanced utilization of the supported carbon-based desulfurization catalyst in each adsorption tower. In particular, the collaborative configuration of the hydrogen sulfide regeneration branch 8 and the pretreatment regeneration branch 9 not only achieves the cyclic regeneration of the desulfurization catalyst but also ensures the resource utilization of sulfur through the directional recovery of desorbed gas. The entire system, through the organic connection and intelligent control of its various functional units, simultaneously completes the entire process of tar removal, organic sulfur conversion, hydrogen sulfide adsorption, and sulfur recovery under low-pressure conditions. Its modular switching mechanism and pressure balance design effectively solve the problems of flow deviation and blockage in traditional processes, giving the system the comprehensive advantages of high processing efficiency, good operational stability, and low energy consumption.

[0083] Finally, it should be noted that although the above embodiments have been described in the text and drawings of this utility model, this should not limit the scope of patent protection of this utility model. Any technical solutions resulting from equivalent structural or procedural substitutions or modifications made based on the essential concept of this utility model and utilizing the content described in the text and drawings of this utility model, as well as the direct or indirect application of the technical solutions of the above embodiments to other related technical fields, are all included within the scope of patent protection of this utility model.

Claims

1. A coke oven gas desulfurization system, characterized in that, include: A gas pressurization unit is connected to the gas inlet pipeline, and the gas pressurization unit is used to pressurize the coke oven gas to 5-30 kPa. The pretreatment unit is connected to the output end of the gas pressurization unit. The pretreatment unit includes multiple pretreatment towers arranged in parallel. Each pretreatment tower is filled with a combination of activated carbon and coke. Each pretreatment tower is equipped with a programmable valve group at its inlet and outlet. The waste heat recovery unit is connected to the pretreatment unit; An organic sulfur conversion unit is connected to the pretreatment unit and is also connected to the waste heat recovery unit. The organic sulfur conversion unit includes at least two organic sulfur conversion towers arranged in parallel, and each organic sulfur conversion tower is filled with a hydrolysis catalyst. A gas heater is connected to the organic sulfur conversion unit; A gas cooler is connected to the output of the organic sulfur conversion unit; The hydrogen sulfide adsorption unit is connected to the output end of the gas cooler. The hydrogen sulfide adsorption unit includes multiple hydrogen sulfide adsorption towers arranged in parallel. The hydrogen sulfide adsorption towers are filled with supported carbon-based desulfurization catalysts. The hydrogen sulfide regeneration branch connects the hydrogen sulfide adsorption unit and the sulfur production equipment, and is used to send the desorbed gas from the adsorption tower to the sulfur production equipment.

2. The coke oven gas desulfurization system according to claim 1, characterized in that, The gas pressurization unit is configured as a centrifugal fan or a Roots blower; The number of the gas pressurization units is two or three; When there are two gas pressurization units, the two gas pressurization units are configured in a one-in-one-standby mode. When the number of gas pressurization units is three, the three gas pressurization units are configured in a two-in-one standby mode.

3. The coke oven gas desulfurization system according to claim 1, characterized in that, The program-controlled valve group includes at least one of a pneumatic shut-off valve, an electric regulating valve, a pressure sensor, and a control unit.

4. The coke oven gas desulfurization system according to claim 3, characterized in that, The pneumatic shut-off valve and the electric regulating valve are connected in parallel. The control unit is electrically connected to the pneumatic shut-off valve, the electric regulating valve, and the pressure sensor, respectively.

5. The coke oven gas desulfurization system according to claim 1, characterized in that, The porosity of the activated carbon and coke composition is configured to be 40% to 65%.

6. The coke oven gas desulfurization system according to claim 1, characterized in that, The waste heat recovery unit is configured as a tubular heat exchanger or a plate heat exchanger.

7. The coke oven gas desulfurization system according to claim 1, characterized in that, The hydrogen sulfide regeneration branch also includes: A desorption pressurizing fan is connected to the hydrogen sulfide adsorption unit; The desorption gas heater is connected to the output end of the desorption pressurizing blower and is used to heat the desorption gas.

8. The coke oven gas desulfurization system according to claim 1, characterized in that, Also includes: The pretreatment regeneration branch is connected between the pretreatment unit and the gas pressurization unit, and is used to send the desorbed gas from the pretreatment tower back to the gas pressurization unit.

9. The coke oven gas desulfurization system according to claim 1, characterized in that, The hydrogen sulfide adsorption unit further includes: The tower body pressure balancing pipeline connects to the top of each hydrogen sulfide adsorption tower installed in parallel; Differential pressure detectors are installed on the inlet and outlet pipelines of each hydrogen sulfide adsorption tower.

10. The coke oven gas desulfurization system according to claim 1, characterized in that, The waste heat recovery unit includes: Multiple heat exchanger modules are connected in parallel; A switching valve group includes multiple switching valves, each of which is respectively installed at the connection end of each heat exchanger module and is used to control the operation status of each heat exchanger module. The backflush line is connected between the outlet of the gas pressurization unit and the heat exchanger module.

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