A dry hydrogen sulfide removal tower for blast furnace gas

Abstract

The present invention provides a dry desulfurization tower for blast furnace gas, the dry desulfurization tower comprises a tower body, the top of the tower body is provided with an air inlet, a catalyst zone and an air outlet zone are provided at the bottom of the tower body, one end of the catalyst zone and one end of the air outlet zone are fixedly connected to the bottom of the tower body, and the air outlet zone is sleeved inside the catalyst zone, the other end of the air outlet zone is externally connected to the air outlet, and a feed hole and a discharge hole are provided on one side of the axial direction of the tower body, and the discharge hole is connected to the catalyst zone on the side facing the inside of the tower body. The dry desulfurization tower of the present invention changes the traditional axial packing tower into a radial packing, reduces the resistance in the tower, makes the catalyst fully contact with the coal gas, and has a high purification efficiency; the overall structure is simple, the strength is high, the adaptability to working conditions is good, the operating rate is high, the mass transfer area is large, and the pressure drop is small, which can significantly improve the efficiency of desulfurization of blast furnace gas.

Description

Technical Field

[0001] The invention belongs to the technical field of dry desulfurization equipment and relates to a dry desulfurization hydrogen tower for blast furnace gas. Background Art

[0002] The sulfides in blast furnace gas are mainly COS and H2S. COS is difficult to remove. Currently, the most commonly used method is to first hydrolyze COS into H2S, and then remove it together with the original H2S in the blast furnace gas.

[0003] CN110591769A discloses a catalytic desulfurization device and method for blast furnace gas, including a cooling tower, an absorption tower, a regeneration tower, a heat exchanger, and a steam boiler. The core of the device is a wet desulfurization process. Although the device can realize the recovery of sulfur resources, the process is complicated, the equipment is large, the alkali consumption is high, the system resistance is large, and the operating cost is also high.

[0004] CN110791328A discloses a blast furnace gas dry desulfurization system and method, including two sets of parallel desulfurization hydrogen towers, one set can be operated and the other can be regenerated, and they can be used alternately to achieve uninterrupted operation. The fixed bed has a smaller processing capacity than the moving bed, the catalyst utilization rate is low, and the energy consumption of in-situ regeneration is also high.

[0005] At present, in order to solve the above-mentioned problems of the prior art, it is urgent to design and develop a new type of dry hydrogen sulfide removal tower for blast furnace gas to improve the desulfurization quality to meet the needs of actual industrial production. Summary of the invention

[0006] In view of the deficiencies in the prior art, the object of the present invention is to provide a dry dehydrogen sulfide tower for blast furnace gas. In the present invention, the traditional axial packing tower is changed to a radial packing tower through the proposed dry dehydrogen sulfide tower, thereby reducing the resistance in the tower, making the catalyst fully contact with the gas, and the catalyst utilization rate is high, and the purification efficiency is high; the overall structure is simple, the strength is high, the adaptability to working conditions is good, the operating rate is high, the mass transfer area is large, and the pressure drop is small, which can significantly improve the efficiency of dehydrogen sulfide of blast furnace gas and has considerable economic benefits.

[0007] To achieve this object, the present invention adopts the following technical solutions:

[0008] The present invention provides a dry dehydrogen sulfide tower for blast furnace gas, the dry dehydrogen sulfide tower comprises a tower body, the top of the tower body is provided with an air inlet, the bottom of the tower body is provided with a catalyst zone and a gas outlet zone, one end of the catalyst zone and one end of the gas outlet zone are fixedly connected to the bottom of the tower body, and the gas outlet zone is sleeved inside the catalyst zone, the other end of the gas outlet zone is externally connected to the gas outlet, and the axial side surface of the tower body is provided with a feed hole and a discharge hole, and the discharge hole is connected to the catalyst zone toward one side inside the tower body.

[0009] In the present invention, through the proposed dry dehydrogen sulfide tower, the traditional axial packing tower is changed into a radial packing tower, the resistance in the tower is reduced, and the catalyst is fully in contact with the coal gas, the catalyst utilization rate is high, and the purification efficiency is high; the overall structure is simple, the strength is high, the adaptability to working conditions is good, the operating rate is high, the mass transfer area is large, and the pressure drop is small, which can significantly improve the efficiency of blast furnace gas dehydrogen sulfide, and has considerable economic benefits.

[0010] It should be noted that in the blast furnace gas dry desulfurization tower described in the present invention, the blast furnace gas enters the tower from the top of the tower, radially passes through the catalyst zone, and flows out from the gas outlet zone in the center of the tower. Compared with the traditional axial feeding method, it occupies a small area. Under the same catalyst loading and gas processing volume, the radial reactor size is smaller than the axial reactor; the resistance is small. Due to the radial flow of the gas, the path through the bed is much shorter than that of the axial reactor, the ventilation cross-sectional area is large, and the gas linear velocity is small, that is, when the bed volume is constant, the pressure drop of the fluid flowing through the bed is proportional to the 2 to 3 powers of the flow channel distance L, so the radial bed resistance is very small; it is easy to scale up. Usually, the bed height of the axial reactor is limited by the bed pressure drop, and its diameter is limited by equipment manufacturing and transportation conditions. It is generally difficult to scale up. The radial flow reactor can increase the axial height of the bed to meet the large-scale requirements of the device under low pressure drop conditions.

[0011] As a preferred technical solution of the present invention, the diameter of the catalyst zone is smaller than the diameter of the tower body.

[0012] Preferably, the height of the catalyst zone is smaller than the height of the tower body.

[0013] Preferably, an annular cavity is formed between the outer surface of the catalyst zone and the inner wall of the tower body.

[0014] Preferably, the annular cavity is a transition zone.

[0015] It should be noted that the transition zone in the present invention is mainly used to rectify and balance the flow field in the tower.

[0016] As a preferred technical solution of the present invention, the width of the transition zone is 5 to 12% of the diameter of the tower body, for example, it can be 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0017] The present invention limits the width of the transition zone to 5 to 12% of the diameter of the tower body because the width of the transition zone affects the volume space velocity of the catalyst in the tower and has a direct impact on the size of the tower pressure drop. If it is not within the numerical range of the present invention, it will lead to a larger volume space velocity of the catalyst in the tower and an increased tower pressure drop under the same tower body. This is due to the imbalance of the structure and flow field in the tower.

[0018] As a preferred technical solution of the present invention, the diameter of the catalyst zone is 60-80% of the diameter of the tower body, for example, it can be 60%, 62%, 64%, 66%, 68%, 70%, 72%, 74%, 76%, 78%, 80%, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0019] The present invention limits the diameter of the catalyst zone to 60-80% of the diameter of the tower body because the diameter of the catalyst zone directly determines the volumetric space velocity. If it is not within the numerical range of the present invention, the purification effect will be reduced and the expected index will not be achieved.

[0020] As a preferred technical solution of the present invention, the diameter of the gas outlet zone is 10-15% of the diameter of the tower body, for example, it can be 10%, 10.5%, 11%, 11.5%, 12%, 12.5%, 13%, 13.5%, 14%, 14.5%, 15%, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0021] The diameter of the gas outlet zone is limited to 10-15% of the diameter of the tower body in the present invention because of the need to control the flow rate in the gas outlet zone and to stabilize the pressure field in the tower. If it is not within the numerical range of the present invention, the overall pressure difference of the tower will increase and the resistance will increase, which is due to the turbulence of the flow field in the tower.

[0022] Preferably, at least one deflection cone is provided in the gas outlet area.

[0023] It should be noted that the specific structure of the baffle cone of the present invention can be a cone or a triangular cone structure.

[0024] As a preferred technical solution of the present invention, the top of the catalyst zone and the inner wall of the tower body close to the air inlet form a cavity, and the cavity is the air inlet zone.

[0025] Preferably, at least one layer of baffles is provided in the air inlet area.

[0026] It should be noted that the present invention does not specifically limit the shape, size and material of the baffles, and those skilled in the art can make adaptive adjustments according to actual conditions. Among them, the shape of the baffles can be rectangular, square, etc.

[0027] As a preferred technical solution of the present invention, a catalyst is arranged in the catalyst zone.

[0028] Preferably, the catalyst is a desulfurizing agent.

[0029] Preferably, the catalyst is in the shape of any one of spherical, cylindrical, sheet or honeycomb, or a combination of two or more thereof.

[0030] It should be noted that the shape of the catalyst in the present invention is any one of spherical, cylindrical, sheet or honeycomb, or a combination of two or more. This is because under this structure, the purification effect can be guaranteed, the pressure drop in the tower is small, and it is easy to load and unload, which is conducive to later maintenance and replacement. Among them, honeycomb-shaped catalysts are more preferred.

[0031] Preferably, the desulfurizing agent is any one of iron oxide, zinc oxide and activated carbon, or a combination of two or more thereof.

[0032] As a preferred technical solution of the present invention, the total filling amount of the catalyst accounts for 65-85% of the volume of the tower, for example, it can be 65%, 67%, 69%, 70%, 72%, 74%, 76%, 78%, 80%, 83%, 85%, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0033] The present invention limits the total filling amount of the catalyst to 65-85% of the volume of the tower because the volume space velocity is guaranteed while taking into account the small pressure drop of the tower and the small total resistance of the system. If it is not within the numerical range of the present invention, it will lead to an imbalance between the volume space velocity and the pressure drop, poor purification effect and high resistance. This is because the flow field in the tower is turbulent and the pressure field is unbalanced.

[0034] Preferably, the volume space velocity of the catalyst is 270-3000h -1 , for example, it can be 270h -1 、300h -1 , 500h -1 、700h -1 、800h -1 , 900h -1 、1000h -1 , 1200h -1 , 1400h -1 , 1600h -1 , 1800h -1 , 2000h -1 、2200h -1 , 2400h -1 、2600h -1 、2800h -1、3000h -1 , but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0035] The present invention defines the volume space velocity of the catalyst as 270-3000h -1 , because it is determined according to different gas volumes, hydrogen sulfide concentrations and catalysts of different shapes. If it is not within the numerical range of the present invention, it will lead to poor purification effect and large system resistance. This is because the amount of catalyst is not matched with the corresponding volume space velocity.

[0036] As a preferred technical solution of the present invention, the tower body is a cylindrical tower body.

[0037] Preferably, the pressure in the tower body is 0.015-0.025 MPa, for example, it can be 0.015 MPa, 0.016 MPa, 0.017 MPa, 0.018 MPa, 0.019 MPa, 0.02 MPa, 0.021 MPa, 0.022 MPa, 0.023 MPa, 0.024 MPa, 0.025 MPa, but is not limited to the listed values, and other unlisted values ​​within the numerical range are equally applicable.

[0038] The pressure in the tower body is limited to 0.015-0.025 MPa in the present invention because it meets the requirements of the rear section entering the pipeline network, so that the rear section does not need to be equipped with a gas booster machine, thereby reducing energy consumption. If it is not within the numerical range of the present invention, the blast furnace gas cannot enter the pipeline network or the energy consumption is high, which is due to the mismatch between the front and rear pressures.

[0039] Preferably, the tower body is arranged at the power output end of the TRT residual pressure power generation device.

[0040] It should be noted that the tower body is set at the power output end of the TRT residual pressure power generation device. The general process is: hydrolysis tower → TRT residual pressure power generation device → dehydrogen sulfide tower → gas tank / pipeline / user.

[0041] Preferably, sealing elements are provided on both the air inlet and the air outlet.

[0042] Preferably, the sealing member is a sealing valve.

[0043] It should be noted that the sealing member is designed in the present invention because the gas area cannot leak.

[0044] As a preferred technical solution of the present invention, at least one circle of baffle plates is provided at the connection between the gas outlet zone and the catalyst zone, and at least one circle of baffle plates is provided at the connection between the transition zone and the catalyst zone.

[0045] Preferably, the partition group includes a plurality of louver partitions.

[0046] Preferably, the plurality of louver partitions are staggered to form the partition group.

[0047] It should be noted that the present invention does not specifically limit the shape, size and material of the louver partition, and those skilled in the art can make adaptive adjustments according to actual conditions. Among them, the shape of the louver partition can be rectangular, square, etc.

[0048] It should be noted that the number of "several" in the present invention is not particularly limited, and can be 10, 20, 30, 40, 50 or 60. The specific number of applications depends on the size of the overall device and is configured accordingly, which should be known to those skilled in the art.

[0049] Compared with the prior art, the present invention has the following beneficial effects:

[0050] In the present invention, through the proposed dry dehydrogen sulfide tower, the traditional axial packing tower is changed into a radial packing tower, the resistance in the tower is reduced, and the catalyst is fully in contact with the coal gas, the catalyst utilization rate is high, and the purification efficiency is high; the overall structure is simple, the strength is high, the adaptability to working conditions is good, the operating rate is high, the mass transfer area is large, and the pressure drop is small, which can significantly improve the efficiency of blast furnace gas dehydrogen sulfide, and has considerable economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0051] Figure 1 A schematic structural diagram of a dry hydrogen sulfide removal tower for blast furnace gas provided in one specific embodiment of the present invention;

[0052] Among them, 1-air inlet zone; 2-transition zone; 3-catalyst zone; 4-air outlet zone; 5-air inlet; 6-air outlet; 7-feed hole; 8-discharge hole. DETAILED DESCRIPTION

[0053] It should be understood that, in the description of the present invention, the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention. In addition, the terms "first", "second", etc. are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first", "second", etc. may explicitly or implicitly include one or more of the features. In the description of the present invention, unless otherwise specified, "multiple" means two or more.

[0054] It should be noted that in the description of the present invention, unless otherwise clearly specified and limited, the terms "disposed", "connected", 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 mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected 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 the present invention can be understood by specific circumstances.

[0055] Those skilled in the art should understand that the present invention necessarily includes necessary pipelines, conventional valves and general pump equipment for realizing a complete process, but the above content does not belong to the main inventive point of the present invention. Those skilled in the art can add layouts on their own based on the process flow and equipment structure selection, and the present invention does not make special requirements and specific limitations on this.

[0056] The technical solution of the present invention is further described below with reference to the accompanying drawings and through specific implementation methods.

[0057] In one embodiment, the present invention provides a dry desulfurization tower for blast furnace gas, such as Figure 1 As shown, the dry dehydrogen sulfide tower includes a tower body, the top of the tower body is provided with an air inlet 5, the bottom of the tower body is provided with a catalyst zone 3 and an air outlet zone 4, one end of the catalyst zone 3 and one end of the air outlet zone 4 are fixedly connected to the bottom of the tower body, and the air outlet zone 4 is sleeved inside the catalyst zone 3, and the other end of the air outlet zone 4 is externally connected to the air outlet 6, and the axial side surface of the tower body is provided with a feed hole 7 and a discharge hole 8, and the discharge hole 8 is connected to the catalyst zone 3 toward one side of the tower body.

[0058] In the present invention, through the proposed dry dehydrogen sulfide tower, the traditional axial packing tower is changed into a radial packing tower, the resistance in the tower is reduced, and the catalyst is fully in contact with the coal gas, the catalyst utilization rate is high, and the purification efficiency is high; the overall structure is simple, the strength is high, the adaptability to working conditions is good, the operating rate is high, the mass transfer area is large, and the pressure drop is small, which can significantly improve the efficiency of blast furnace gas dehydrogen sulfide, and has considerable economic benefits.

[0059] It should be noted that in the dry desulfurization tower for blast furnace gas of the present invention, blast furnace gas enters the tower from the top of the tower, radially passes through the catalyst zone 3, and then flows out from the gas outlet zone 4 in the center of the tower. Compared with the traditional axial feeding method, it occupies a small area. Under the same catalyst loading and gas processing volume, the radial reactor size is smaller than the axial reactor; the resistance is small. Due to the radial flow of gas, the path through the bed is much shorter than that of the axial reactor, the ventilation cross-sectional area is large, and the gas linear velocity is small, that is, when the bed volume is constant, the pressure drop of the fluid flowing through the bed is proportional to the 2 to 3 powers of the flow channel distance L, so the radial bed resistance is very small; it is easy to scale up. Usually, the bed height of the axial reactor is limited by the bed pressure drop, and its diameter is limited by equipment manufacturing and transportation conditions. It is generally difficult to scale up. The radial flow reactor can increase the axial height of the bed to meet the large-scale requirements of the device under low pressure drop conditions.

[0060] The diameter of the catalyst zone 3 is smaller than the diameter of the tower body, and the height of the catalyst zone 3 is smaller than the height of the tower body. An annular cavity is formed between the outer surface of the catalyst zone 3 and the inner wall of the tower body, and the annular cavity is the transition zone 2.

[0061] The width of the transition zone 2 is 5-12% of the diameter of the tower body, for example, 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0062] The diameter of the catalyst zone 3 is 60-80% of the diameter of the tower body, for example, it can be 60%, 62%, 64%, 66%, 68%, 70%, 72%, 74%, 76%, 78%, 80%, but it is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0063] The diameter of the gas outlet zone 4 is 10-15% of the diameter of the tower body, for example, it can be 10%, 10.5%, 11%, 11.5%, 12%, 12.5%, 13%, 13.5%, 14%, 14.5%, 15%, but it is not limited to the listed values, and other values ​​not listed in the numerical range are also applicable. At least one baffle cone is arranged in the gas outlet zone 4.

[0064] The top of the catalyst zone 3 and the inner wall of the tower body near the air inlet 5 form a cavity, which is the air inlet zone 1. At least one layer of baffles is provided in the air inlet zone 1. It should be noted that the present invention does not specifically limit the shape, size and material of the baffles, and those skilled in the art can make adaptive adjustments according to actual conditions. Among them, the shape of the baffles can be rectangular, square, etc.

[0065] The catalyst zone 3 is provided with a catalyst, which is a desulfurizing agent, and the catalyst is in the shape of any one of sphere, cylinder, sheet or honeycomb, or a combination of two or more thereof. The desulfurizing agent is any one of iron oxide, zinc oxide and activated carbon, or a combination of two or more thereof.

[0066] The total filling amount of the catalyst accounts for 65-85% of the volume of the tower, for example, it can be 65%, 67%, 69%, 70%, 72%, 74%, 76%, 78%, 80%, 83%, 85%, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0067] The volume space velocity of the catalyst is 270-3000h -1 , for example, it can be 270h -1 、300h -1 , 500h -1 、700h -1 、800h -1 , 900h -1 、1000h -1 , 1200h -1 , 1400h -1 , 1600h -1 , 1800h -1 , 2000h -1 、2200h -1 , 2400h -1 、2600h -1 、2800h -1 、3000h -1 , but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0068] The tower body is a cylindrical tower body, and the pressure inside the tower body is 0.015-0.025 MPa, for example, it can be 0.015 MPa, 0.016 MPa, 0.017 MPa, 0.018 MPa, 0.019 MPa, 0.02 MPa, 0.021 MPa, 0.022 MPa, 0.023 MPa, 0.024 MPa, 0.025 MPa, but is not limited to the listed values, and other unlisted values ​​within the numerical range are equally applicable.

[0069] The tower body is set at the power output end of the TRT residual pressure power generation device. It should be noted that the tower body is set at the power output end of the TRT residual pressure power generation device. The general process is: hydrolysis tower → TRT residual pressure power generation device → desulfurization tower → gas tank / pipeline network / user.

[0070] The air inlet 5 and the air outlet 6 are both provided with seals, which are sealing valves. At least one baffle group is provided at the connection between the air outlet zone 4 and the catalyst zone 3, and at least one baffle group is provided at the connection between the transition zone 2 and the catalyst zone 3. The baffle group includes a plurality of louver baffles, and the plurality of louver baffles are staggered to form a baffle group.

[0071] It should be noted that the present invention does not specifically limit the shape, size and material of the louver partition, and those skilled in the art can make adaptive adjustments according to actual conditions. Among them, the shape of the louver partition can be rectangular, square, etc.

[0072] It should be noted that the number of "several" in the present invention is not particularly limited, and can be 10, 20, 30, 40, 50 or 60. The specific number of applications depends on the size of the overall device and is configured accordingly, which should be known to those skilled in the art.

[0073] Example 1

[0074] This embodiment provides a dry desulfurization tower for blast furnace gas, wherein:

[0075] The dry desulfurization hydrogen tower includes a tower body, the top of the tower body is provided with an air inlet 5, the bottom of the tower body is provided with a catalyst zone 3 and an air outlet zone 4, one end of the catalyst zone 3 and one end of the air outlet zone 4 are fixedly connected to the bottom of the tower body, and the air outlet zone 4 is sleeved inside the catalyst zone 3, and the other end of the air outlet zone 4 is externally connected to the air outlet 6, and the axial side surface of the tower body is provided with a feed hole 7 and a discharge hole 8, and the discharge hole 8 is connected to the catalyst zone 3 toward one side of the tower body, and the tower body is arranged at the power output end of the TRT residual pressure power generation device.

[0076] The diameter of the catalyst zone 3 is smaller than the diameter of the tower body, and the height of the catalyst zone 3 is smaller than the height of the tower body. An annular cavity is formed between the outer surface of the catalyst zone 3 and the inner wall of the tower body, and the annular cavity is the transition zone 2.

[0077] The width of the transition zone 2 is 8% of the diameter of the tower body, the diameter of the catalyst zone 3 is 70% of the diameter of the tower body, and the diameter of the gas outlet zone 4 is 12% of the diameter of the tower body.

[0078] The top of the catalyst zone 3 and the inner wall of the tower body near the air inlet 5 form a cavity, which is the air inlet zone 1. A layer of baffles is arranged in the air inlet zone 1. The catalyst zone 3 is provided with a catalyst, which is a desulfurizer, and the catalyst is spherical in shape, and the desulfurizer is activated carbon.

[0079] The total filling amount of the catalyst accounts for 70% of the volume of the tower, and the volumetric space velocity of the catalyst is 1200h -1 The tower body is a cylindrical tower body, and the pressure inside the tower body is 0.02MPa.

[0080] The air inlet 5 and the air outlet 6 are both provided with seals, which are sealing valves. A circle of baffles is provided at the connection between the air outlet zone 4 and the catalyst zone 3, and a circle of baffles is provided at the connection between the transition zone 2 and the catalyst zone 3. The baffle group includes 80 louver baffles, and the 80 louver baffles are staggered to form a baffle group.

[0081] Example 2

[0082] This embodiment provides a dry desulfurization tower for blast furnace gas, wherein:

[0083] The dry desulfurization hydrogen tower includes a tower body, the top of the tower body is provided with an air inlet 5, the bottom of the tower body is provided with a catalyst zone 3 and an air outlet zone 4, one end of the catalyst zone 3 and one end of the air outlet zone 4 are fixedly connected to the bottom of the tower body, and the air outlet zone 4 is sleeved inside the catalyst zone 3, and the other end of the air outlet zone 4 is externally connected to the air outlet 6, and the axial side surface of the tower body is provided with a feed hole 7 and a discharge hole 8, and the discharge hole 8 is connected to the catalyst zone 3 toward one side of the tower body, and the tower body is arranged at the power output end of the TRT residual pressure power generation device.

[0084] The diameter of the catalyst zone 3 is smaller than the diameter of the tower body, and the height of the catalyst zone 3 is smaller than the height of the tower body. An annular cavity is formed between the outer surface of the catalyst zone 3 and the inner wall of the tower body, and the annular cavity is the transition zone 2.

[0085] The width of the transition zone 2 is 5% of the diameter of the tower body, the diameter of the catalyst zone 3 is 60% of the diameter of the tower body, and the diameter of the gas outlet zone 4 is 10% of the diameter of the tower body.

[0086] The top of the catalyst zone 3 and the inner wall of the tower body near the air inlet 5 form a cavity, which is the air inlet zone 1. Two layers of baffles are arranged in the air inlet zone 1. The catalyst zone 3 is provided with a catalyst, which is a desulfurizer, and has a honeycomb shape, and the desulfurizer is iron oxide.

[0087] The total filling amount of the catalyst accounts for 65% of the volume of the tower, and the volumetric space velocity of the catalyst is 270h -1 The tower body is a cylindrical tower body, and the pressure inside the tower body is 0.015MPa.

[0088] The air inlet 5 and the air outlet 6 are both provided with seals, which are sealing valves. Two circles of baffle groups are provided at the connection between the air outlet zone 4 and the catalyst zone 3, and two circles of baffle groups are provided at the connection between the transition zone 2 and the catalyst zone 3. The baffle group includes 60 louver baffles, and the 60 louver baffles are staggered to form a baffle group.

[0089] Example 3

[0090] This embodiment provides a dry desulfurization tower for blast furnace gas, wherein:

[0091] The dry desulfurization hydrogen tower includes a tower body, the top of the tower body is provided with an air inlet 5, the bottom of the tower body is provided with a catalyst zone 3 and an air outlet zone 4, one end of the catalyst zone 3 and one end of the air outlet zone 4 are fixedly connected to the bottom of the tower body, and the air outlet zone 4 is sleeved inside the catalyst zone 3, and the other end of the air outlet zone 4 is externally connected to the air outlet 6, and the axial side surface of the tower body is provided with a feed hole 7 and a discharge hole 8, and the discharge hole 8 is connected to the catalyst zone 3 toward one side of the tower body, and the tower body is arranged at the power output end of the TRT residual pressure power generation device.

[0092] The diameter of the catalyst zone 3 is smaller than the diameter of the tower body, and the height of the catalyst zone 3 is smaller than the height of the tower body. An annular cavity is formed between the outer surface of the catalyst zone 3 and the inner wall of the tower body, and the annular cavity is the transition zone 2.

[0093] The width of the transition zone 2 is 12% of the diameter of the tower body, the diameter of the catalyst zone 3 is 80% of the diameter of the tower body, and the diameter of the gas outlet zone 4 is 15% of the diameter of the tower body.

[0094] The top of the catalyst zone 3 and the inner wall of the tower body near the air inlet 5 form a cavity, which is the air inlet zone 1. Two layers of baffles are arranged in the air inlet zone 1. The catalyst zone 3 is provided with a catalyst, which is a desulfurizer, and has a honeycomb shape, and the desulfurizer is iron oxide.

[0095] The total filling amount of the catalyst accounts for 85% of the volume of the tower, and the volumetric space velocity of the catalyst is 300h -1 The tower body is a cylindrical tower body, and the pressure inside the tower body is 0.025MPa.

[0096] The air inlet 5 and the air outlet 6 are both provided with seals, which are sealing valves. The connection between the air outlet zone 4 and the catalyst zone 3 is provided with three circles of baffle groups, and the connection between the transition zone 2 and the catalyst zone 3 is provided with three circles of baffle groups, which include 100 louver baffles, and the 100 louver baffles are staggered to form a baffle group.

[0097] Example 4

[0098] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Embodiment 1 is that the width of the transition zone is 4% of the diameter of the tower body. Other parameters and test conditions are the same as those in the embodiment.

[0099] Example 5

[0100] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Embodiment 1 is that the width of the transition zone is 13% of the diameter of the tower body. Other parameters and test conditions are the same as those in the embodiment.

[0101] Example 6

[0102] This embodiment provides a dry dehydrogen sulfide tower for blast furnace gas. The difference from Embodiment 1 is that the diameter of the catalyst zone is 50% of the diameter of the tower body. Other parameters and test conditions are the same as those in the embodiment.

[0103] Example 7

[0104] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Embodiment 1 is that the diameter of the catalyst zone is 90% of the diameter of the tower body. Other parameters and test conditions are the same as those in the embodiment.

[0105] Example 8

[0106] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Embodiment 1 is that the diameter of the gas outlet zone is 8% of the diameter of the tower body. Other parameters and test conditions are the same as those in the embodiment.

[0107] Example 9

[0108] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Embodiment 1 is that the diameter of the gas outlet zone is 16% of the diameter of the tower body. Other parameters and test conditions are the same as those in the embodiment.

[0109] Example 10

[0110] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Embodiment 1 is that the total filling amount of the catalyst accounts for 60% of the volume of the tower. Other parameters and test conditions are the same as those in the embodiment.

[0111] Embodiment 11

[0112] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Embodiment 1 is that the total filling amount of the catalyst accounts for 90% of the volume of the tower. Other parameters and test conditions are the same as those in the embodiment.

[0113] Example 12

[0114] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Example 1 is that the volumetric space velocity of the catalyst is 250h -1 , other parameters and test conditions are the same as those in the embodiment.

[0115] Embodiment 13

[0116] This embodiment provides a dry desulfurization tower for blast furnace gas. The difference from Embodiment 1 is that the volumetric space velocity of the catalyst is 3200 h -1 , other parameters and test conditions are the same as those in the embodiment.

[0117] Comparative Example 1

[0118] This comparative example provides a dry desulfurization tower for blast furnace gas. The difference from Example 1 is that an air inlet is arranged at the bottom of the tower body, and other parameters and test conditions are the same as those in the example.

[0119] Comparative Example 2

[0120] This comparative example provides a dry desulfurization tower for blast furnace gas. The difference from Example 1 is that an air inlet is arranged on the side of the tower body, and other parameters and test conditions are the same as those in the example.

[0121] The desulfurization effect of the dry hydrogen sulfide removal tower in the above embodiments and comparative examples was tested. The specific testing method includes: using gas chromatography to analyze the concentration of hydrogen sulfide before and after desulfurization, further calculating the desulfurization efficiency, and using a differential pressure sensor to test the resistance of the tower. The results are shown in Table 1 below.

[0122] Table 1

[0123] Examples and Comparative Examples Desulfurization efficiency (%) Tower resistance (kPa) Example 1 98 0.7 Example 2 99 0.8 Example 3 99 0.7 Example 4 97 1 Example 5 97 0.9 Example 6 97 0.9 Example 7 96 1 Example 8 97 0.9 Example 9 97 0.9 Example 10 95 0.9 Embodiment 11 94 1.1 Example 12 93 0.9 Embodiment 13 95 0.9 Comparative Example 1 93 1.2 Comparative Example 2 92 1.3

[0124] It can be seen from Table 1 above:

[0125] By comparing Example 1 with Examples 4 and 5, it can be seen that the treatment efficiency of the dry dehydrogen sulfide tower in Example 1 is higher than that of the dry dehydrogen sulfide tower in Examples 4 and 5, and the resistance of the dry dehydrogen sulfide tower in Example 1 is lower than that of the dry dehydrogen sulfide tower in Examples 4 and 5. This is because the present invention limits the width of the transition zone to 5 to 12% of the diameter of the tower body, so that the flow field in the tower is balanced, the resistance is small, the blast furnace gas passes through the catalyst layer evenly and stably, and the catalyst utilization rate is high.

[0126] By comparing Example 1 with Examples 6 and 7, it can be seen that the treatment efficiency of the dry dehydrogen sulfide tower in Example 1 is higher than that of the dry dehydrogen sulfide tower in Examples 6 and 7, and the resistance of the dry dehydrogen sulfide tower in Example 1 is lower than that of the dry dehydrogen sulfide tower in Examples 6 and 7. This is because the present invention limits the diameter of the catalyst zone to 60-80% of the diameter of the tower body, so that the blast furnace gas and the catalyst layer have a suitable contact time, which is not too long or too short, which is conducive to full utilization of the catalyst and reduction of tower resistance.

[0127] By comparing Example 1 with Examples 8 and 9, it can be seen that the treatment efficiency of the dry dehydrogen sulfide tower in Example 1 is higher than the treatment efficiency of the dry dehydrogen sulfide tower in Examples 8 and 9, and the resistance of the dry dehydrogen sulfide tower in Example 1 is lower than the resistance of the dry dehydrogen sulfide tower in Examples 8 and 9. This is because the present invention limits the diameter of the gas outlet zone to 10-15% of the diameter of the tower body, so that the gas flow rate in the gas outlet zone is not too high or too low, affecting the flow field in the tower.

[0128] By comparing Example 1 with Examples 10 and 11, it can be seen that the treatment efficiency of the dry dehydrogen sulfide tower in Example 1 is higher than the treatment efficiency of the dry dehydrogen sulfide tower in Examples 10 and 11, and the resistance of the dry dehydrogen sulfide tower in Example 1 is lower than the resistance of the dry dehydrogen sulfide tower in Examples 10 and 11. This is because the present invention limits the total filling amount of the catalyst to 65-85% of the volume of the tower, so that under the same tower volume, the tower resistance is optimized under the premise of ensuring the desulfurization effect.

[0129] By comparing Example 1 with Examples 12 and 13, it can be seen that the treatment efficiency of the dry dehydrogen sulfide tower in Example 1 is higher than that of the dry dehydrogen sulfide tower in Examples 12 and 13, and the resistance of the dry dehydrogen sulfide tower in Example 1 is lower than that of the dry dehydrogen sulfide tower in Examples 12 and 13. This is because the volume space velocity of the catalyst is limited to 270-3000h / min in the present invention. -1 , so that the volume space velocity and the tower resistance are balanced. Under different volume space velocities, the tower resistance is the smallest.

[0130] By comparing Example 1 with Comparative Examples 1 and 2, it can be seen that the processing efficiency of the dry dehydrogen sulfide tower in Example 1 is higher than that of the dry dehydrogen sulfide tower in Comparative Examples 1 and 2, and the resistance of the tower is small. This is because the present invention balances the flow field in the tower by limiting the air inlet to the top of the tower, rather than the bottom or side of the tower.

[0131] The above description is only a specific implementation mode of the present invention, but the protection scope of the present invention is not limited thereto. Those skilled in the art should understand that any changes or substitutions that can be easily thought of by those skilled in the art within the technical scope disclosed by the present invention are within the protection scope and disclosure scope of the present invention.

Claims

1. A dry desulfurization tower for blast furnace gas, characterized in that: The dry desulfurization hydrogen tower comprises a tower body, the top of the tower body is provided with an air inlet, the bottom of the tower body is provided with a catalyst zone and an air outlet zone, one end of the catalyst zone and one end of the air outlet zone are fixedly connected to the bottom of the tower body, and the air outlet zone is sleeved inside the catalyst zone, the other end of the air outlet zone is externally connected to the air outlet, and a feed hole and a discharge hole are provided on one axial side surface of the tower body, and the discharge hole is connected to the catalyst zone toward one side inside the tower body; The height of the catalyst zone is smaller than the height of the tower body, an annular cavity is formed between the outer surface of the catalyst zone and the inner wall of the tower body, the annular cavity is a transition zone, and the width of the transition zone is 5 to 12% of the diameter of the tower body; The diameter of the catalyst zone is 60-80% of the diameter of the tower body, the diameter of the gas outlet zone is 10-15% of the diameter of the tower body, the top of the catalyst zone and the inner wall of the tower body close to the air inlet form a cavity, and the cavity is the air inlet zone.

2. The dry desulfurization tower according to claim 1, characterized in that: The diameter of the catalyst zone is smaller than the diameter of the tower body.

3. The dry desulfurization tower according to claim 1, characterized in that: At least one deflection cone is arranged in the gas outlet area.

4. The dry desulfurization tower according to claim 1, characterized in that: At least one layer of baffles is arranged in the air inlet area.

5. The dry desulfurization tower according to claim 1, characterized in that: A catalyst is arranged in the catalyst zone.

6. The dry desulfurization tower according to claim 5, characterized in that: The catalyst is a desulfurizing agent.

7. The dry desulfurization tower according to claim 5, characterized in that: The catalyst is in the shape of any one of sphere, cylinder, sheet or honeycomb, or a combination of two or more thereof.

8. The dry desulfurization tower according to claim 7, characterized in that: The catalyst is any one of iron oxide, zinc oxide and activated carbon or a combination of two or more thereof.

9. The dry desulfurization tower according to claim 8, characterized in that: The total filling amount of the catalyst accounts for 65-85% of the volume in the tower.

10. The dry desulfurization tower according to claim 9, characterized in that: The volume space velocity of the catalyst is 270-3000h -1 .

11. The dry desulfurization tower according to claim 1, characterized in that: The tower body is a cylindrical tower body.

12. The dry desulfurization tower according to claim 1, characterized in that: The pressure in the tower body is 0.015-0.025 MPa.

13. The dry desulfurization tower according to claim 1, characterized in that: The tower body is arranged at the power output end of the TRT residual pressure power generation device.

14. The dry desulfurization tower according to claim 1, characterized in that: The air inlet and the air outlet are both provided with sealing members.

15. The dry desulfurization tower according to claim 14, characterized in that: The sealing element is a sealing valve.

16. The dry desulfurization tower according to claim 1, characterized in that: At least one circle of baffle plates is disposed at the connection between the gas outlet zone and the catalyst zone, and at least one circle of baffle plates is disposed at the connection between the transition zone and the catalyst zone.

17. The dry dehydrogen sulfide tower according to claim 16, characterized in that: The partition plate group includes a plurality of louver partition plates.

18. The dry desulfurization tower according to claim 17, characterized in that: The plurality of louver partitions are arranged in a staggered manner to form the partition group.

Images