CN114515500A - Device and method for removing blast furnace gas hydrogen sulfide - Google Patents
Device and method for removing blast furnace gas hydrogen sulfide Download PDFInfo
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- CN114515500A CN114515500A CN202210252121.XA CN202210252121A CN114515500A CN 114515500 A CN114515500 A CN 114515500A CN 202210252121 A CN202210252121 A CN 202210252121A CN 114515500 A CN114515500 A CN 114515500A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B7/00—Blast furnaces
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- B01D2251/00—Reactants
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- B01D2251/304—Alkali metal compounds of sodium
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention relates to a device and a method for removing blast furnace gas hydrogen sulfide, the device comprises an absorption device, an alkali liquor device, a process water device, an oxidation regeneration device and a sulfur refining device, the alkali liquor consumption is reduced by specifically setting each component and specifically setting the flow and parameters of the method using the device, the zero discharge of wastewater is approached, the problems of low airspeed and large floor area caused by the existing process are solved, and the technical effects of small floor area, simple operation, no influence on the use of subsequent equipment of a blast furnace and the like are realized under the condition of ensuring the desulfurization rate.
Description
Technical Field
The invention belongs to the field of comprehensive treatment of metallurgical waste gas, and particularly relates to a device and a method for removing blast furnace gas hydrogen sulfide.
Background
With the increasing environmental protection consciousness and the increasing requirements for energy conservation and emission reduction in the iron and steel industry, the tail end treatment mode is commonly adopted in the blast furnace gas desulfurization at present, namely, the SO in the tail end flue gas after the blast furnace gas user burns is removed2However, the blast furnace gas user sites are scattered, and the desulfurization facilities need to be arranged at multiple points The problems of repeated investment, high operation cost and the like exist, and meanwhile, the amount of flue gas generated after the blast furnace gas is combusted by a terminal user is large, so that the blast furnace gas is not suitable for the environmental protection requirement under the new situation. The blast furnace gas fine desulfurization is implemented through a source treatment technology, the content of sulfur in the gas can be reduced through centralized treatment before each user uses the blast furnace gas, the gas amount treated by the source treatment is only about 60% of the flue gas amount after the user burns, the blast furnace gas fine desulfurization method has the characteristics of low total investment, small total occupied area, low operation cost, contribution to centralized management and the like, the pressure of tail end desulfurization can be relieved, the scale of tail end desulfurization is reduced, and the corrosion of the sulfur in the blast furnace gas to a transmission pipeline and equipment is avoided, so that the research on a process suitable for the blast furnace gas fine desulfurization is meaningful from the source treatment.
The blast furnace gas contains CO and CO2、N2、H2And trace amount of sulfide. The sulfide in the blast furnace gas is organic sulfur and inorganic sulfur, and the total sulfur concentration is 100-200mg/Nm3. The organic sulfur mainly comprises carbonyl sulfide (COS) and a small amount of carbon disulfide (CS)2) Inorganic sulfur with hydrogen sulfide (H)2S) is the main component, and a small amount of sulfur dioxide is also contained. At present, the main flow process of blast furnace gas fine desulfurization comprises the following three processes: the process 1 comprises the following steps: hydrolysis + TRT + alkaline absorption (NaOH) acid-base neutralization (wet process); and (2) a process: hydrolysis + TRT + alkali absorption (Na) 2CO3) Wet oxidation (wet process); and (3) a process: TRT + hydrolysis + absorption (dry process). For the hydrolysis part, COS is hydrolyzed into H by the three processes2S, the efficiency is ensured to a certain extent. The main difference lies in the back end H2And (4) S removal process. In the process 1, NaOH is used as an alkali source for absorption, and hydrogen sulfide in the coal gas is removed in an acid-base neutralization mode. Its advantages are high absorption efficiency, high air speed, small space occupied by absorption tower, and high content of CO in blast furnace gas2Resulting in high lye consumption. In the process 2, Na is used as an absorbent2CO3As an alkali source and a certain amount of catalyst is added, the process uses the process of removing hydrogen sulfide (PDS) from coke oven gas for reference, hydrogen sulfide in the gas is oxidized into elemental sulfur, and the hydrogen sulfide is removed by the processes of filter pressing, a sulfur melting kettle and the like, and the process has the advantages of ensuring absorption efficiency, ensuring wastewater waste water absorption efficiency and ensuring the quality of the wastewaterThe discharge amount is less, and the defects are that the process airspeed is lower because the gas flow of the blast furnace gas is larger than that of the coke oven gas, but the sulfur content is lower, a plurality of towers are required to be connected in parallel, the occupied area is larger, and no site exists for more enterprises. And in the process 3, the active carbon base or the iron base is used as a desulfurizing agent, and hydrogen sulfide in the coal gas is removed from the coal gas in a chemical adsorption mode. The advantages are high absorption rate, no waste water, low airspeed, large occupied area, high pressure drop, poor working condition adaptability, limited by sulfur capacity and large waste agent production.
In combination with the current actual operation conditions of industrial enterprises, the three processes for fine desulfurization of coal gas still have no process route and equipment suitable for blast furnace gas desulfurization in the hydrogen sulfide absorption section on the premise of stable hydrolysis efficiency. Especially, the dry hydrogen sulfide removal process is difficult to advance if the process cannot overcome the difficulties due to the complexity of the blast furnace gas atmosphere, the variability of working conditions, the limitation of the adsorbent and the like. Therefore, the wet removal of the hydrogen sulfide in the blast furnace gas is the leading direction of future development, and how to solve the problems existing in the wet method at present is a main factor for restricting the further development of the blast furnace gas fine desulfurization.
Disclosure of Invention
In order to solve the defects of the wet hydrogen sulfide removal process, the invention combines the traditional alkali method (NaOH source) hydrogen sulfide removal process and the coke oven gas hydrogen sulfide removal process, organically combines the two processes together and improves the two processes, thereby providing the device and the method for removing the blast furnace gas hydrogen sulfide.
The method is realized by the following technical scheme:
a device for removing blast furnace gas hydrogen sulfide comprises an absorption device, an alkali liquor device, a process water device, an oxidation regeneration device and a sulfur refining device.
The absorption device comprises an absorption tower body, a distributor plate, a spraying layer, a demister, a backwashing layer, a circulating pump and a circulating water tank; the spraying layer is horizontally arranged in the absorption tower body and is provided with a plurality of layers, each layer of spraying layer is formed by arranging densely arranged nozzles, the distributor plate is horizontally arranged in the absorption tower body below the spraying layer and is used for uniformly distributing gas of blast furnace gas entering the absorption tower body, one or more layers of backwashing layers are arranged in the absorption tower body above the spraying layer, one or more demisters are arranged in the absorption tower body above the backwashing layers, a blast furnace gas inlet is formed in the side wall of the absorption tower body below the distributor plate, an overflow port is formed in the side wall of the absorption tower body below the blast furnace gas inlet, and a treated gas exhaust port is formed in the top end of the absorption tower body; the circulating water tank is provided with a circulating water outlet and a regenerated liquid inlet, the circulating water outlet is communicated with the liquid inlet of the spraying layer through a pipeline, and a circulating pump is arranged on the pipeline.
The alkali liquor device comprises a desulfurizer storage tank and a desulfurizer metering pump, the desulfurizer storage tank is used for storing desulfurizer liquid, the desulfurizer storage tank is provided with a desulfurizer liquid outlet, the desulfurizer liquid outlet is communicated with one or more layers of liquid inlets on the upper part of the spraying layer through a pipeline, and the desulfurizer metering pump is arranged on the pipeline.
The process water device comprises a process water tank and a process water pump, wherein the process water tank is provided with a process water replenishing port and a process water discharging port, the process water replenishing port is connected with an external process water pipe network through a pneumatic valve, the process water discharging port is communicated with a liquid inlet of the backwashing layer through a pipeline, and the pipeline is provided with the process water pump.
The oxidation regeneration device comprises a rich liquid pool, a rich liquid pump, ejectors and a regeneration pool, wherein the rich liquid pool is used for temporarily storing desulfurization liquid overflowing from the bottom of the absorption tower body, the rich liquid pool comprises a rich liquid pool body, a rich liquid inlet and a rich liquid outlet, the rich liquid inlet and the rich liquid outlet are respectively arranged on the side wall of the rich liquid pool body, the rich liquid inlet is communicated with the overflow port through a pipeline, the regeneration pool comprises a regeneration pool body, an ejection inlet, a foam discharge port and a regeneration water outlet, the ejection inlet is arranged at the top of the regeneration pool body, a plurality of ejectors are arranged at the ejection inlet, the inlet of each ejector is communicated with the rich liquid outlet through a pipeline, the rich liquid pump is arranged on the pipeline, the ejectors are self-suction ejectors, and are used for sucking air, mixing the air with the desulfurization liquid discharged from the rich liquid outlet and then ejecting the air into the regeneration pool body, the foam discharge port is arranged at the top end of one side wall of the regeneration tank body, a foam overflow weir is arranged in the regeneration tank body from the foam discharge port, a regeneration water outlet is arranged on one side wall of the regeneration tank body, and the regeneration water outlet is communicated with the regeneration liquid inlet of the circulating water tank through a pipeline.
The sulfur refining device comprises a sulfur foam tank, a sulfur foam pump and a filter press; the sulfur foam tank comprises a tank inlet, a tank outlet and a stirrer, wherein the tank inlet is communicated with the foam discharge port of the regeneration tank through a pipeline, the stirrer is arranged in the sulfur foam tank, the tank outlet is communicated with the inlet of the filter press through a pipeline, and the pipeline is provided with the sulfur foam pump.
Preferably, the spraying layer is provided with 4 layers; the number of the demisters is 2, the number of the backwashing layers is 3, the demisters and the backwashing layers are arranged at intervals, the uppermost layer is 1 demister, the middle layer is provided with 2 backwashing layers, then 1 demister is arranged, and the lowest part is provided with 1 backwashing layer; the pipeline of each spraying layer is provided with one circulating pump, and the circulating pumps are arranged in parallel; and a radar liquid level meter A is arranged in the circulating water tank.
Preferably, the desulfurizer liquid outlet is communicated with the liquid inlets of the upper 1 st layer and the upper 2 nd layer in the multiple spraying layers through pipelines.
Preferably, a radar liquid level meter B is further arranged in the process water tank, and the pneumatic valve and the radar liquid level meter B are controlled in an interlocking mode; the process water pump is provided with 2, and 1 uses another 1 for standby.
Preferably, the regeneration tank is arranged above the rich liquid tank, and a radar liquid level meter C is arranged in the rich liquid tank body; the rich liquid pump is provided with 3, 2 use 1 spare, and the flow of single pump is 1/2 of total circulation volume, and the lift is 65 m.
Preferably, the sulfur foam pump is provided with 2 sulfur foam pumps, 1 sulfur foam pump is used, the other sulfur foam pump is used for standby, and the flow rate of the single sulfur foam pump is 15-30m3H, the lift is 60 m; the filter press is a plate and frame filter press, and the filter press area is 80-120 square meters.
The method for removing the hydrogen sulfide from the blast furnace gas by adopting the device comprises the following steps:
(1) preparing an alkaline desulfurization solution with the pH of 8-9 and the catalyst content of 2-4 g/L, wherein the alkali source is sodium carbonate or sodium hydroxide, and injecting the prepared alkaline desulfurization solution into a circulating water tank and a conical hopper at the bottom of an absorption tower body, wherein the injection amount of the circulating water tank is 60-70% of the volume of the circulating water tank, and the injection amount in the conical hopper of the absorption tower body is until an overflow port overflows.
(2) Starting a plurality of circulating pumps connected in parallel in sequence, wherein the starting sequence is that the lower layer is started first, then the circulating pumps are started in sequence from bottom to top, and when the liquid level in the rich liquid pool reaches a set threshold value, the rich liquid pump is started; and then opening a blast furnace gas inlet so that the blast furnace gas is discharged into the absorption tower body.
(3) The gas flow velocity in the absorption tower body is 2-3 m/s, the liquid-gas ratio is 2-4, the gas flow is uniformly distributed through a distributor plate, the hydrogen sulfide in the blast furnace gas is in countercurrent full contact with the desulfurization liquid sprayed by the spraying layer to generate acid-base neutralization reaction, the hydrogen sulfide in the blast furnace gas is absorbed, the sprayed liquid flows into a cone at the bottom of the absorption tower body and then flows into a rich liquid tank through the overflow port, the desulfurized blast furnace gas passes through a demister from the top of the absorption tower body to remove mechanical water, and the concentration of the hydrogen sulfide in the treatment gas is less than or equal to 15mg/Nm3The treated gas enters the gas pipe network through the treated gas outlet and is sent to downstream users.
(4) After being pressurized by a pregnant solution pump, the liquid in the pregnant solution pool automatically sucks air through a plurality of self-suction ejectors, the liquid in the pregnant solution pool and the sucked air are in parallel flow, and then the liquid is discharged to the bottom of a regeneration pool through a throat pipe, a diffusion pipe and a tail pipe of the ejectors to complete the oxidation regeneration of the desulfurization catalyst, and the regenerated circulating liquid returns to a circulating water pool through a regenerated water outlet in a natural overflow mode; the sulfur foam generated at the top of the regeneration tank during the spraying process overflows through the foam overflow weir, and then is discharged into the sulfur foam tank through the foam discharge port by utilizing the potential difference.
(5) And the sulfur foam entering the sulfur foam tank is stirred by a stirrer in the sulfur foam tank, then is sent to a plate-and-frame filter press by a sulfur foam pump to generate a filter cake, and clear liquid is returned to the circulating water tank.
(6) When the pressure difference of the demister exceeds 195-205 pa, starting the process water pump, and performing backwashing through the backwashing layer; and when the pH value in the circulating water pool is less than 8.0 (the operation range is controlled to be 8.0-9.0), starting a desulfurizer metering pump, and pumping the desulfurizer in a desulfurizer storage tank into one or more layers of liquid inlets at the middle upper part of the spraying layer.
Preferably, the injection amount of the circulating water pool in the step (1) is 2/3 of the volume of the circulating water pool; the effective volume of the circulating water pool is set to 1/2 of the total circulating volume.
Preferably, in the step (3), the atomized particle size of the nozzle in the spray layer is 200-500 μm, the pressure is 0.2-0.5 MPa, and the single-layer coverage area is 125-200%.
Preferably, in the step (4), the desulfurization solution is pressurized by a rich solution pump and automatically sucks air through a plurality of ejectors at the top of the regeneration tank, and the desulfurization solution and the air flow through two phases of the ejectors and the throats, the diffusion pipe and the tail part to enter the regeneration tank, so that the oxidative regeneration of the desulfurization catalyst is completed.
The invention has the technical effects that:
The invention improves the traditional technology for removing hydrogen sulfide by a wet method (NaOH) and removing hydrogen sulfide by PDS (coke oven gas) so as to form the technology suitable for removing hydrogen sulfide by blast furnace gas. The desulfurization solution is recycled by adopting single tower, high space velocity and multi-layer spraying and combining with the oxidation regeneration process of sulfur ions, thereby not only solving the problems of large wastewater amount and large alkali liquor consumption caused by the hydrogen sulfide removal by the traditional alkaline method, but also solving the problems of low space velocity and large occupied area caused by complex components, large gas amount and different working conditions of blast furnace gas and coke oven gas.
The method solves the problems of the prior technology for removing hydrogen sulfide by blast furnace gas fine desulfurization and land occupation and the like by adopting the parameters of high space velocity (2-3 m/s) and small liquid-gas ratio (2-4) and matching with a reasonably arranged desulfurization circulating liquid oxidation regeneration process. By setting high airspeed and low liquid-gas ratio, the number of absorption towers and the occupied area are greatly reduced, and the pressure drop of an absorption system is reduced because no filler is used. By the arrangement of the oxidation regeneration method, the desulfurization solution can be recycled, so that the consumption of alkali liquor is reduced, and the discharge amount of wastewater is close to zero emission.
The device has the advantages that the overall structure is simple, the adaptability is strong, the device can adapt to the content of different hydrogen sulfide for treatment only by adjusting the spraying amount of the first layer of alkaline desulfurization solution, the occupied area is small under the condition of ensuring the desulfurization rate, the operation is simple, and the subsequent equipment use of the blast furnace is not influenced.
Drawings
FIG. 1 is a schematic process flow diagram of the method for removing blast furnace gas hydrogen sulfide of the present invention.
Wherein: 101-absorption tower body, 102-back flushing layer, 103-spraying layer, 104-overflow port, 105-circulating water pool, 106-circulating pump, 201-desulfurizing agent storage tank and 202-desulfurizing agent metering pump; 301-a process water tank, 302-a process water pump, 401-a liquid-rich pool, 402-a regeneration pool, 403-a foam overflow weir, 404-a liquid-rich pump, 405-an ejector, 501-a foam tank, 502-a sulfur foam pump, 503-a filter press, 601-a sulfur powder storage tank, A-blast furnace gas, B-outside water, C-byproducts and D-are communicated with a gas pipe network.
Detailed Description
The technical scheme of the invention is further explained by combining the drawings and the embodiment:
example 1
The device for removing the blast furnace gas hydrogen sulfide shown in figure 1 comprises an absorption device, an alkali liquor device, a process water device, an oxidation regeneration device and a sulfur refining device. Wherein the blast furnace gas is initially divided into two branches, a branch valve group is arranged on a bypass which is extended upwards in the figure 1, when the device for removing the blast furnace gas and the hydrogen sulfide is overhauled on line or has other requirements, the branch valve group is opened, and the gas directly enters a pipe network.
The absorption device comprises an absorption tower body, a distributor plate, a spraying layer, a demister, a backwashing layer, a circulating pump and a circulating water tank; the spray layer is horizontally arranged in the absorption tower body and is provided with a plurality of layers, each layer of spray layer is formed by densely arranging nozzles, the distributor plate is horizontally arranged in the absorption tower body below the spray layer and is used for uniformly distributing gas of blast furnace gas entering the absorption tower body, one or more layers of back wash layers are arranged in the absorption tower body above the spray layer, one or more demisters are arranged in the absorption tower body above the back wash layers, the demisters and the back wash layers are arranged at intervals, the uppermost layer is provided with 1 demister, the middle part is provided with 2 back wash layers, then 1 demister is arranged, and the lowest part is provided with 1 back wash layer; a blast furnace gas inlet is formed in the side wall of the absorption tower body below the distributor plate, an overflow port is formed in the side wall of the absorption tower body below the blast furnace gas inlet, and a treated gas exhaust port is formed in the top end of the absorption tower body; the circulating water tank is provided with a circulating water outlet and a regenerated liquid inlet, the circulating water outlet is communicated with the liquid inlet of the spraying layer through a pipeline, and a circulating pump is arranged on the pipeline. In this embodiment, 4 spraying layers are provided, a circulation pump (i.e. 4 circulation pumps, which are a circulation pump a, a circulation pump B, a circulation pump C, and a circulation pump D in sequence from bottom to top) is provided on the pipeline of each spraying layer, the circulation pumps are arranged in parallel (not shown in fig. 1), the tower diameter of the absorption tower is determined by controlling the empty tower gas velocity by 2-3m/s according to the gas volume of the blast furnace gas, and the tower height is controlled by the number of spraying layers and demister layers; the distributor plate uniformly distributes the blast furnace gas entering the tower; the spraying layer 4 is connected with a circulating water pool; the atomizing particle size of the nozzle is 200-; 2 layers of demisters are matched with 3 layers of backwashing, the backwashing time is set to be automatic flushing according to the pressure difference of the demisters, and the flushing water comes from a process water device; 4 circulating pumps, wherein the flow of a single pump is determined according to the liquid-gas ratio of 2-4, and the lift is determined according to the height of each spraying layer, the pressure required by the nozzles and the pipeline loss; the effective volume of the circulating water pool is 1/2 of the total circulating quantity, and a radar liquid level meter is arranged; the bottom of the absorption tower is provided with an overflow pipe.
The alkali liquor device comprises a desulfurizer storage tank and a desulfurizer metering pump, the desulfurizer storage tank is used for storing desulfurizer liquid, the desulfurizer storage tank is provided with a desulfurizer liquid outlet, the desulfurizer liquid outlet is communicated with one or more layers of liquid inlets on the upper part of the spraying layer through pipelines, and the desulfurizer metering pump is arranged on the pipeline. The desulfurizer storage tank of this embodiment is 1, underground, effective volume 5 is upright, sets up the radar level gauge. 2 desulfurizer metering pumps are connected with the first layer spraying layer and the second layer spraying layer of the absorption tower, the lift is determined according to the height of the first layer spraying layer of the absorption tower, the pressure required by a nozzle and the pipeline loss, and the flow is added according to the sulfur content in the gas.
The process water device comprises a process water tank and a process water pump, wherein the process water tank is provided with a process water replenishing port and a process water discharging port, the process water replenishing port is connected with an external process water pipe network through a pneumatic valve, the process water discharging port is communicated with a liquid inlet of the backwashing layer through a pipeline, and the pipeline is provided with the process water pump. The process water tank of this embodiment sets up the radar level gauge, and the moisturizing mouth passes through the pneumatic valve with the process water pipe net outdoors and links to each other, and this pneumatic valve uses interlocking control with the radar level gauge. And 2 process water pumps, one used and one spare, are connected with a back flushing pipeline of a demister at the top layer of the absorption tower.
The oxidation regeneration device comprises a rich liquid pool, a rich liquid pump, ejectors and a regeneration pool, wherein the rich liquid pool is used for temporarily storing desulfurization liquid overflowing from the bottom of the absorption tower body, the rich liquid pool comprises a rich liquid pool body, a rich liquid inlet and a rich liquid outlet, the rich liquid inlet and the rich liquid outlet are respectively arranged on the side wall of the rich liquid pool body, the rich liquid inlet is communicated with the overflow port through a pipeline, the regeneration pool comprises a regeneration pool body, an injection inlet, a foam discharge port and a regenerated water outlet, the injection inlet is arranged at the top of the regeneration pool body, a plurality of ejectors are arranged at the injection inlet, the inlets of the ejectors are communicated with the rich liquid outlet through pipelines, the rich liquid pump is arranged on the pipeline, the ejectors are self-suction ejectors, the ejectors are used for sucking air and mixing with the desulfurization liquid discharged from the rich liquid outlet and then ejecting the air into the regeneration pool body, the foam discharge port is arranged at the top end of one side wall of the regeneration tank body, a foam overflow weir is arranged in the regeneration tank body from the foam discharge port, a regenerated water outlet is arranged on one side wall of the regeneration tank body, and the regenerated water outlet is communicated with the regenerated liquid inlet of the circulating water tank through a pipeline. The pregnant solution pump of this embodiment is provided with 3, two-purpose one, and the pump flow of single pump is 1/2 of total circulation volume, head 65 m. The desulfurization solution is pressurized by a rich solution pump and automatically sucks air through a plurality of ejectors at the top of the regeneration tank, the desulfurization solution and the air flow in parallel through an ejector throat pipe, a diffusion pipe and the tail part and enter the regeneration tank, and the oxidative regeneration of the desulfurization catalyst is completed. And suspended sulfur particles in the regeneration pool are floated by air to form sulfur foam, and the sulfur foam overflows from a foam overflow weir at the top of the regeneration pool and enters a sulfur foam tank.
The sulfur refining device comprises a sulfur foam tank, a sulfur foam pump and a filter press; the sulfur foam tank comprises a tank inlet, a tank outlet and a stirrer, wherein the tank inlet is communicated with the foam discharge port of the regeneration tank through a pipeline, the stirrer is arranged in the sulfur foam tank, the tank outlet is communicated with the inlet of the filter press through a pipeline, and the pipeline is provided with the sulfur foam pump. The sulfur foam pump of this example was equipped with 2 pumps, one for one and one for standby, with a flow rate of 15-30m3H, head 60 m. The filter pressing area of the plate and frame filter press is 80-120 square meters.
Example 2
This example, using the apparatus of example 1, includes: (1) preparing an alkaline desulfurization solution with the pH of 8-9 and the catalyst content of 2-4 g/L, wherein the alkali source is sodium carbonate/sodium hydroxide, and injecting the prepared alkaline desulfurization solution into a circulating water tank and a conical hopper at the bottom of an absorption tower body, wherein the injection amount of the circulating water tank is 2/3 of the volume of the circulating water tank, and the injection amount in the conical hopper of the absorption tower body is until an overflow port overflows.
(2) The method comprises the steps of starting a plurality of circulating pumps connected in parallel in sequence, starting the lower layer in sequence, then starting the circulating pumps from bottom to top in sequence (namely the circulating pump A, the circulating pump B, the circulating pump C and the circulating pump D from bottom to top in sequence), starting the pregnant solution pump when the liquid level in the pregnant solution tank reaches a set threshold value (the threshold value can be set to 2/3 of the height of the pregnant solution tank, for example, when the pregnant solution tank is 6m, the threshold value can be set to 4m), and then putting the desulfurization absorption device and the oxidation regeneration device into operation completely. Then opening the inlet and outlet blind plate valves of the absorption device in sequence, opening the inlet butterfly valve, the outlet butterfly valve, slowly closing the bypass blind plate valve, opening the blast furnace gas inlet, allowing the gas to enter the absorption tower, and starting the full-scale operation of the desulfurization device.
(3) The gas flow velocity in the absorption tower body is 2-3 m/s (the average value is about 2.8 m/s), the liquid-gas ratio is 2-4 (the average value is about 2.6), the gas flow is uniformly distributed through a distributor plate, the hydrogen sulfide in the blast furnace gas is fully contacted with the desulfurization liquid sprayed by a spraying layer in a countercurrent manner to generate acid-base neutralization reaction, the hydrogen sulfide in the blast furnace gas is absorbed, the sprayed liquid flows into a cone hopper at the bottom of the absorption tower body and then flows into a rich liquid tank through an overflow port, the desulfurized blast furnace gas has the concentration of the hydrogen sulfide in the treatment gas of less than or equal to 15mg/Nm after mechanical water is removed from the top of the absorption tower body through a demister, and the concentration of the hydrogen sulfide in the treatment gas is less than or equal to 15mg/Nm3The treated gas enters the gas pipe network through the treated gas outlet and is sent to downstream users.
(4) After being pressurized by a pregnant solution pump, the liquid in the pregnant solution pool automatically sucks air through a plurality of self-suction ejectors, the liquid in the pregnant solution pool and the sucked air are in parallel flow, and then the liquid is discharged to the bottom of a regeneration pool through a throat pipe, a diffusion pipe and a tail pipe of the ejectors to complete the oxidation regeneration of the desulfurization catalyst, and the regenerated circulating liquid returns to a circulating water pool through a regenerated water outlet in a natural overflow mode; the sulfur foam generated at the top of the regeneration tank during the spraying process overflows through the foam overflow weir, and then is discharged into the sulfur foam tank through the foam discharge port by utilizing the potential difference.
(5) And the sulfur foam entering the sulfur foam tank is stirred by a stirrer in the sulfur foam tank, then is conveyed to a plate-and-frame filter press by a sulfur foam pump to generate a filter cake, and clear liquid is returned to the circulating water tank.
(6) When the pressure difference of the demister exceeds 200pa, starting the process water pump, and performing back washing through a back washing layer; and (3) checking the concentration (whether the checked pH value is in a range of 2-4 g/L) and the pH value of the catalyst in the circulating liquid every day, starting a desulfurizer metering pump when the pH value in the circulating water pool is less than 8.0, and pumping the desulfurizer in a desulfurizer storage tank into one or more layers of liquid inlets at the middle upper part of the spraying layer.
Claims (10)
1. A device for removing blast furnace gas hydrogen sulfide is characterized by comprising an absorption device, an alkali liquor device, a process water device, an oxidation regeneration device and a sulfur refining device;
the absorption device comprises an absorption tower body, a distributor plate, a spraying layer, a demister, a backwashing layer, a circulating pump and a circulating water tank; the spraying layer is horizontally arranged in the absorption tower body and is provided with a plurality of layers, each layer of spraying layer is formed by densely arranging nozzles, the distributor plate is horizontally arranged in the absorption tower body below the spraying layer and is used for uniformly distributing gas of blast furnace gas entering the absorption tower body, one or more layers of backwashing layers are arranged in the absorption tower body above the spraying layer, one or more demisters are arranged in the absorption tower body above or at intervals of the backwashing layers, a blast furnace gas inlet is formed in the side wall of the absorption tower body below the distributor plate, an overflow port is formed in the side wall of the absorption tower body below the blast furnace gas inlet, and a treated gas exhaust port is formed in the top end of the absorption tower body; the circulating water tank is provided with a circulating water outlet and a regenerated liquid inlet, the circulating water outlet is communicated with the liquid inlet of the spraying layer through a pipeline, and a circulating pump is arranged on the pipeline;
The alkali liquor device comprises a desulfurizer storage tank and a desulfurizer metering pump, the desulfurizer storage tank is used for storing desulfurizer liquid, the desulfurizer storage tank is provided with a desulfurizer liquid outlet, the desulfurizer liquid outlet is communicated with one or more layers of liquid inlets at the upper part of the multiple spraying layers through a pipeline, and the pipeline is provided with the desulfurizer metering pump;
the process water device comprises a process water tank and a process water pump, wherein the process water tank is provided with a process water replenishing port and a process water discharging port, the process water replenishing port is connected with an external process water pipe network through a pneumatic valve, the process water discharging port is communicated with a liquid inlet of the backwashing layer through a pipeline, and the pipeline is provided with the process water pump;
the oxidation regeneration device comprises a rich liquid pool, a rich liquid pump, ejectors and a regeneration pool, wherein the rich liquid pool is used for temporarily storing desulfurization liquid overflowing from the bottom of the absorption tower body, the rich liquid pool comprises a rich liquid pool body, a rich liquid inlet and a rich liquid outlet, the rich liquid inlet and the rich liquid outlet are respectively arranged on the side wall of the rich liquid pool body, the rich liquid inlet is communicated with the overflow port through a pipeline, the regeneration pool comprises a regeneration pool body, an ejection inlet, a foam discharge port and a regeneration water outlet, the ejection inlet is arranged at the top of the regeneration pool body, a plurality of ejectors are arranged at the ejection inlet, the inlet of each ejector is communicated with the rich liquid outlet through a pipeline, the rich liquid pump is arranged on the pipeline, the ejectors are self-suction ejectors, and are used for sucking air, mixing the air with the desulfurization liquid discharged from the rich liquid outlet and then ejecting the air into the regeneration pool body, the foam discharge port is arranged at the top end of one side wall of the regeneration tank body, a foam overflow weir is arranged in the regeneration tank body at the foam discharge port, a regeneration water outlet is formed in one side wall of the regeneration tank body, and the regeneration water outlet is communicated with the regeneration liquid inlet of the circulating water tank through a pipeline;
The sulfur refining device comprises a sulfur foam tank, a sulfur foam pump and a filter press; the sulfur foam tank comprises a tank inlet, a tank outlet and a stirrer, wherein the tank inlet is communicated with the foam discharge port of the regeneration tank through a pipeline, the stirrer is arranged in the sulfur foam tank, the tank outlet is communicated with the inlet of the filter press through a pipeline, and the pipeline is provided with the sulfur foam pump.
2. The device for removing the blast furnace gas hydrogen sulfide as claimed in claim 1, wherein the spraying layer is provided with 4 layers; the number of the demisters is 2, the number of the backwashing layers is 3, the demisters and the backwashing layers are arranged at intervals, the uppermost layer is 1 demister, the middle layer is provided with 2 backwashing layers, then 1 demister is arranged, and the lowest part is provided with 1 backwashing layer; the pipeline of each spraying layer is provided with one circulating pump, and the circulating pumps are arranged in parallel; and a radar liquid level meter A is arranged in the circulating water tank.
3. The device for removing the blast furnace gas hydrogen sulfide as claimed in claim 1, wherein the desulfurizing agent liquid outlet is communicated with the liquid inlets of the upper 1 st and 2 nd layers in the plurality of spraying layers through pipelines.
4. The device for removing the blast furnace gas hydrogen sulfide according to the claim 1, wherein a radar level gauge B is arranged in the process water tank, and the pneumatic valve and the radar level gauge B are controlled in an interlocking way; the process water pump is provided with 2, and 1 uses another 1 for standby.
5. The device for removing the blast furnace gas hydrogen sulfide as claimed in claim 1, wherein the regeneration tank is arranged above the rich liquor tank, and a radar liquid level meter C is arranged in the rich liquor tank body; the rich liquid pump is provided with 3, 2 use 1 for standby, the flow of a single pump is 1/2 of the total circulating quantity, and the lift is 65 m.
6. A method for removing hydrogen sulfide from blast furnace gas, which is characterized in that the device of any one of claims 1-5 is adopted, and the method comprises the following steps:
(1) preparing an alkaline desulfurization solution with the pH of 8-9 and the catalyst content of 2-4 g/L, wherein the alkali source is sodium carbonate or sodium hydroxide, and injecting the prepared alkaline desulfurization solution into a circulating water tank and a conical hopper at the bottom of an absorption tower body, wherein the injection amount of the circulating water tank is 60-70% of the volume of the circulating water tank, and the injection amount in the conical hopper of the absorption tower body is until an overflow port overflows;
(2) Sequentially starting a plurality of circulating pumps connected in parallel, and starting the liquid enrichment pump when the liquid level in the liquid enrichment pool reaches a set threshold value; then opening a blast furnace gas inlet so that the blast furnace gas is discharged into the absorption tower body;
(3) the gas flow velocity in the absorption tower body is 2-3 m/s, the liquid-gas ratio is 2-4, the gas flow is uniformly distributed through the distributor plate, the hydrogen sulfide in the blast furnace gas is in full countercurrent contact with the desulfurization liquid sprayed on the spraying layer, acid-base neutralization reaction is generated, the hydrogen sulfide in the blast furnace gas is absorbed, and the sprayed liquid flows to the bottom of the absorption tower bodyThe gas flows into a rich liquid pool through the overflow port in the conical hopper, and the desulfurized blast furnace gas passes through a demister from the top of the absorption tower body to remove mechanical water, so that the concentration of hydrogen sulfide in the treatment gas is less than or equal to 15mg/Nm3The treated gas enters a gas pipe network through a treated gas outlet and is sent to downstream users;
(4) after being pressurized by a pregnant solution pump, the liquid in the pregnant solution pool automatically sucks air through a plurality of self-suction ejectors, the liquid in the pregnant solution pool and the sucked air are in parallel flow, and then the liquid is discharged to the bottom of a regeneration pool through a throat pipe, a diffusion pipe and a tail pipe of the ejector to complete the oxidation regeneration of the desulfurization catalyst, and the regenerated circulating liquid returns to a circulating water pool through a regenerated water outlet in a natural overflow mode; sulfur foam generated at the top of the regeneration tank in the spraying process overflows through a foam overflow weir and is discharged into a sulfur foam tank through a foam discharge port by utilizing potential difference;
(5) The sulfur foam entering the sulfur foam tank is stirred by a stirrer in the sulfur foam tank, then is sent to a plate-and-frame filter press by a sulfur foam pump to generate a filter cake, and clear liquid is returned to the circulating water tank;
(6) when the pressure difference of the demister exceeds 195-205 pa, starting the process water pump, and performing backwashing through the backwashing layer; and when the pH value in the circulating water tank is less than 8.0, starting a desulfurizer metering pump, and pumping the desulfurizer in a desulfurizer storage tank into one or more layers of liquid inlets at the middle upper part of the spraying layer.
7. The method for removing the blast furnace gas hydrogen sulfide as claimed in claim 6, wherein in the step (1), the injection amount of the circulating water pool is 2/3 of the volume of the circulating water pool; the effective volume of the circulating water pool is set to 1/2 of the total circulating quantity; in the step (2), the plurality of parallel circulating pumps are started in sequence, and the starting sequence is that the circulating pumps on the lower layer are started firstly and then are started in sequence from bottom to top.
8. The method for removing blast furnace gas hydrogen sulfide as claimed in claim 6, wherein in the step (3), the atomized particle size of the nozzle in the spray layer is about 200-500 μm, the pressure is about 0.2-0.5 MPa, and the single-layer coverage area is about 125-200%.
9. The method for removing the blast furnace gas hydrogen sulfide as claimed in claim 6, wherein the sulfur foam pump is provided with 2 pumps, one pump is used for another pump for standby, and the flow rate of the single sulfur foam pump is 15-30m 3H, the lift is 60 m; the filter press is a plate-and-frame filter press, and the filter pressing area is 80-120 square meters.
10. The method for removing the blast furnace gas hydrogen sulfide according to claim 6, wherein in the step (4), the desulfurization solution is pressurized by a pregnant solution pump and automatically sucks air through a plurality of ejectors arranged at the top of the regeneration tank, and the desulfurization solution and the air flow through a throat, a diffusion pipe and a tail of the ejector in parallel to enter the regeneration tank to complete the oxidative regeneration of the desulfurization catalyst.
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