CN110591769A - Blast furnace gas catalytic desulfurization device and method - Google Patents
Blast furnace gas catalytic desulfurization device and method Download PDFInfo
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- CN110591769A CN110591769A CN201910665699.6A CN201910665699A CN110591769A CN 110591769 A CN110591769 A CN 110591769A CN 201910665699 A CN201910665699 A CN 201910665699A CN 110591769 A CN110591769 A CN 110591769A
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 24
- 230000023556 desulfurization Effects 0.000 title claims abstract description 24
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims abstract description 11
- 239000007789 gas Substances 0.000 claims abstract description 78
- 239000002904 solvent Substances 0.000 claims abstract description 64
- 238000010521 absorption reaction Methods 0.000 claims abstract description 47
- 230000008929 regeneration Effects 0.000 claims abstract description 35
- 238000011069 regeneration method Methods 0.000 claims abstract description 35
- 239000002250 absorbent Substances 0.000 claims abstract description 30
- 230000002745 absorbent Effects 0.000 claims abstract description 30
- 239000003054 catalyst Substances 0.000 claims abstract description 30
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 26
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 18
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 17
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 17
- 239000011593 sulfur Substances 0.000 claims abstract description 15
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 15
- 125000001741 organic sulfur group Chemical group 0.000 claims abstract description 12
- 150000001412 amines Chemical class 0.000 claims abstract description 9
- 150000007524 organic acids Chemical class 0.000 claims abstract description 9
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000006227 byproduct Substances 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 102
- 238000005507 spraying Methods 0.000 claims description 17
- 239000002253 acid Substances 0.000 claims description 16
- 238000005086 pumping Methods 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 5
- 239000002202 Polyethylene glycol Substances 0.000 claims description 4
- 229920001223 polyethylene glycol Polymers 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 6
- 238000004064 recycling Methods 0.000 abstract description 6
- 125000004122 cyclic group Chemical group 0.000 abstract description 2
- 238000000703 high-speed centrifugation Methods 0.000 abstract description 2
- 229910000831 Steel Inorganic materials 0.000 description 8
- 239000010959 steel Substances 0.000 description 8
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 7
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 238000003915 air pollution Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 150000004763 sulfides Chemical class 0.000 description 2
- 239000000956 alloy Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000011152 fibreglass Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
- C10K1/14—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic
Abstract
The invention provides a blast furnace gas catalytic desulfurization device and a method, comprising a cooling tower, an absorption tower, a regeneration tower, a heat exchanger and a steam boiler. Dissolving sulfur dioxide, organic sulfur and hydrogen sulfide in blast furnace gas in an absorption tower in a solvent tank, adding organic acid and an organic amine catalyst to form an active intermediate complex, and reacting with tail gas and the hydrogen sulfide dissolved in the solvent to generate elemental sulfur. The rich solution enters from the top of the regeneration tower and is in countercurrent contact with stripping steam generated by a steam boiler from bottom to top, so that sulfide and CO dissolved in the rich solution are separated2And the obtained barren solution enters an absorption tower again to realize the recycling of the solvent absorbent. The rich solution and the barren solution realize heat exchange in the heat exchanger, the cooled rich solution enters the regeneration tower, and the heated barren solution enters the absorption tower. And (3) cooling a part of catalyst in the reaction process of the regeneration tower to 70 ℃ through a cooler arranged outside the regeneration tower, and then separating steam sulfur and byproducts in the catalyst by high-speed centrifugation, thereby realizing the cyclic utilization of the part of catalyst.
Description
Technical Field
The invention relates to a novel catalytic desulfurization device and a novel catalytic desulfurization method for blast furnace gas, which are applied to organic sulfur removal of the blast furnace gas in a steel plant.
Background
The pollutant emission ratio of sintering machines, pellets and blast furnace units of steel plants in the non-electric industry air pollution treatment is large, the treatment is needed firstly, wherein the flue gas conditions of the sintering machines and the pellets are similar to the conventional process in the electric industry and can be carried out simply according to the treatment route of the air pollution treatment process, but the blast furnace gas is limited by the production process and the flue gas conditions of the blast furnace gas and does not have the rigid emission index requirement on the tail gas by the environmental protection department, the ultralow emission modification working scheme of steel enterprises is released along with the environmental protection department, the ultralow emission modification is completed in the important areas of the long triangle and the like before 10 months in 2020, and the requirement on the pollutant in the blast furnace is SO2：50mg/m3The requirement is greatly stricter than the existing standard, but the market has not performed too much process research on the treatment of blast furnace gas pollutants before, and the blast furnace gas is used as a low-calorific-value fuel, and the sulfur content in the blast furnace gas mainly comprises carbonyl sulfide (COS) and sulfur dioxide (SO)2) Carbon disulfide (CS)2) Mainly, the three sulfur components account for about 90 percent of the total sulfur, wherein carbonyl sulfur accounts for about 30 percent of the total sulfur, and SO2The total sulfur content is 25-30%, CS2The total sulfur content is 30 percent, the S content in blast furnace gas is low (less than 0.01 percent), the components are more and more complex, and in addition, the sulfide treatment difficulty is very large, most steel plants directly send the sulfur into a torch to burn the sulfur, so a large amount of energy is wasted. At present, energy is increasingly scarce and energy conservation and emission reduction are increasingly carried out, the reasonable utilization of blast furnace gas is a necessary trend. In addition, the existence of organic sulfur not only causes the corrosion of equipment and facilities, poisons various catalysts in the subsequent production process, but also seriously threatens the personal safety if the operation is improper, so the desulfurization of the blast furnace gas becomes a key for the utilization of the blast furnace gas and belongs to pollutants which must be eliminated or controlled.
In addition, the ecological damage and the environmental pollution caused by the development and the utilization of coal in China are serious. How to improve the utilization ratio of resources such as coal and the like under the condition of permission of economic conditions and reduce the pollution to the environment makes the problem which needs to be solved urgently, the implementation of clean coal technology is the strategic choice of Chinese energy, and the clean coal technology can solve the problems in three aspects: (1) controlling the discharge amount of pollutants and greenhouse gases; (2) the dependence degree on imported petroleum is reduced; (3) the utilization efficiency is improved.
Disclosure of Invention
The purpose of the invention is: in order to solve the technical bottleneck of the organic sulfur removal of the blast furnace gas in the steel plant at present and realize the technical breakthrough, a novel catalytic desulfurization device and a novel catalytic desulfurization method for the blast furnace gas, which can stably operate for a long time, are provided.
The technical scheme of the invention is as follows:
a blast furnace gas catalytic desulfurization device comprises a cooling tower, an absorption tower, a solvent absorbent tank, a catalyst tank, a first liquid circulating pump and a filter; the air inlet of the cooling tower is connected with the blast furnace tail gas, and the air outlet of the cooling tower is connected with the air inlet of the absorption tower; a first solvent tank is arranged below the air inlet in the absorption tower, and a first gas-liquid contact device, a first spraying device and a first demisting device are sequentially arranged between the air inlet and the air outlet at the top of the absorption tower from bottom to top; the solvent absorbent tank is communicated with the first solvent tank, the catalyst tank and the first solvent tank are both communicated with a liquid inlet of the first liquid circulating pump, a liquid outlet of the first liquid circulating pump is connected with a liquid inlet of the filter, and a liquid outlet of the filter is connected with the first spraying device; the first solvent tank and the solvent absorbent tank are internally provided with solvent absorbents for absorbing sulfur dioxide, organic sulfur and hydrogen sulfide in blast furnace gas, and the catalyst in the catalyst tank is organic acid and organic amine.
The cooling tower is arranged at an inlet at the front end of the absorption tower to humidify the tail gas, the temperature of the blast furnace gas entering the absorption tower is controlled to be 120-130 ℃, sulfur dioxide, organic sulfur and hydrogen sulfide in the blast furnace gas in the absorption tower are dissolved in the first solvent tank, an active intermediate complex is formed by organic acid and an organic amine catalyst which are added through the first liquid circulating pump and a solvent absorbent, and then the active intermediate complex reacts with the tail gas and the hydrogen sulfide dissolved in the solvent to generate elemental sulfur.
Further, the system also comprises a regeneration tower, a heat exchanger, a second liquid circulating pump, a steam boiler and a second spraying device; a second solvent tank is arranged at the bottom in the regeneration tower, and a second demisting device and a second gas-liquid contact device are sequentially arranged between a gas outlet at the top of the regeneration tower and the second solvent tank from top to bottom; the second spraying device is arranged between the demisting device and the second gas-liquid contact device; the first solvent tank is connected with a liquid inlet of a second liquid circulating pump, a liquid outlet of the second liquid circulating pump is connected with a hydrothermal solution inlet of the heat exchanger, and a hydrothermal solution outlet of the heat exchanger is connected with a second spraying device; the liquid inlet of the steam boiler is communicated with the second solvent tank, and the steam outlet is arranged between the second gas-liquid contact device and the second solvent tank.
After the desulfurization rich solution absorbing blast furnace tail gas is pumped out by a second liquid circulating pump and exchanges heat by a heat exchanger to recover partial heat, the rich solution enters from the top of a regeneration tower and is in countercurrent contact with stripping steam generated by a steam boiler from bottom to top at the temperature of 90-130 ℃ and the pressure of-50 kpa, and sulfide and CO dissolved in the rich solution are separated out2. The liquid sulfur is precipitated to the bottom of the second solvent tank.
Further, the device also comprises a third liquid circulating pump and a third spraying device; the third spraying device is arranged in the absorption tower and between the first gas-liquid contact device and the first demisting device; and a liquid inlet of the third liquid circulating pump is communicated with the second solvent tank, a liquid outlet of the third liquid circulating pump is connected with a cold liquid inlet of the heat exchanger, and a cold liquid outlet of the heat exchanger is connected with a third spraying device.
Dissolved sulfides and CO in the pregnant solution2The lean solution obtained after being analyzed enters the absorption tower through a third liquid circulating pump and a third spraying device, so that the recycling of the solvent absorbent is realized. The second liquid circulating pump pumps high-temperature rich liquid into the heat exchanger from the absorption tower, the third liquid circulating pump pumps low-temperature barren liquid into the heat exchanger from the regeneration tower, the rich liquid and the barren liquid realize heat exchange in the heat exchanger, the cooled rich liquid enters the regeneration tower, and the heated barren liquid enters the absorption tower.
Furthermore, a liquid sulfur outlet is arranged at the bottom of the second solvent tank.
Further, the device also comprises a cooler and a high-speed centrifugal separator; the liquid inlet of the cooler is communicated with the second solvent tank, the liquid outlet of the cooler is connected with the high-speed centrifugal separator, and the liquid outlet of the high-speed centrifugal separator is connected with the catalyst tank.
And in the reaction process of the regeneration tower, part of the catalyst is regenerated, and after the temperature is reduced to 70 ℃ by a cooler arranged outside the tower, liquid sulfur and byproducts in the catalyst are separated by high-speed centrifugation, so that the cyclic utilization of part of the catalyst is realized.
Further, a gas outlet at the top of the regeneration tower is connected with a regenerated acid gas incineration system.
And the regenerated acid gas tower top demisting device from the top of the regeneration tower removes liquid drops, then the liquid drops are conveyed to an acid gas incineration system through a draught fan, and the acid gas is exhausted into the atmosphere after incineration.
Preferably, the solvent absorbent is a mixture of polyethylene glycol and water.
Preferably, the applicable load range of the novel catalytic desulfurization device for blast furnace gas is 30-100%.
Preferably, the pre-cooling tower, the absorption solvent absorption tower and the regeneration tower are in steel structure type and are all in a reverse spray washing mode.
Preferably, the first liquid circulating pump, the second liquid circulating pump and the third liquid circulating pump are all centrifugal pumps made of horizontal alloy materials.
Preferably, the defogging device is a device which is made of a PP plate and is in a multi-channel hook shape to separate liquid drops carried by tail gas.
Preferably, the high-speed centrifugal separator can separate the catalyst by-products by different settling speeds according to different centrifugal forces applied to the solution with different specific gravities.
Preferably, the absorbent solution filter is a basket type external pipeline filter, and the spraying device is in a uniform distribution type of a glass fiber reinforced plastic pipe network;
preferably, the packing device in the absorption tower is combined into a certain pattern by adopting PP baffle plates and then used for increasing the contact residence time of the solvent absorbent and the blast furnace tail gas.
A blast furnace gas catalytic desulfurization method comprises the following steps:
step 1: cooling blast furnace gas by a cooling tower;
step 2: the blast furnace gas enters an absorption tower to contact with a solvent absorbent, sulfur dioxide, organic sulfur and hydrogen sulfide are dissolved in the solvent absorbent, the solvent absorbent reacts with a catalyst to form an active intermediate complex, and the active intermediate complex reacts with the hydrogen sulfide in the solvent absorbent to generate elemental sulfur; circularly pumping the solution at the bottom of the absorption tower into the upper part of the absorption tower;
and step 3: the solution at the bottom of the absorption tower is cooled by a heat exchanger and then is circularly pumped into the upper part of a regeneration tower to be in countercurrent contact with stripping steam generated by a steam boiler from bottom to top, and the dissolved sulfide and CO are separated out2；
And 4, step 4: circularly pumping the solution at the bottom of the regeneration tower into a heat exchanger, exchanging heat with the solution in the absorption tower in the heat exchanger, and then entering the absorption tower;
and 5: circularly pumping the solution at the bottom of the regeneration tower into a cooler, cooling, and then feeding the solution into a high-speed centrifugal separator to separate out a catalyst and a byproduct;
step 6: removing liquid drops of the regenerated acid gas from the top of the regeneration tower through a tower top demisting device, conveying the regenerated acid gas to an acid gas incineration system through a draught fan, and discharging the regenerated acid gas after incineration; and removing liquid drops from the gas in the absorption tower through a tower top demisting device and then discharging the gas.
The invention has the beneficial effects that: the design of the invention controls the temperature of the tail gas to be 120-130 ℃ through the pre-cooling tower, and the gas-liquid absorption ratio of the solvent absorbent reaches 1: 200, the consumption of polyethylene glycol serving as an absorbent is low, and the desulfurization device of the organic acid organic amine catalyst is designed, so that the conversion rate of the device to COS and CS2 is improved, the problems of low solubility of hydrogen sulfide and emulsification of NaSO4 and sulfur are solved, the long-term stable operation of the novel catalytic desulfurization device for the blast furnace gas is ensured, the regeneration and recycling of the solvent absorbent and part of the catalyst are realized, the operation cost can be greatly saved, and a better process technical path is provided for the desulfurization of the blast furnace gas in the steel plant in the future.
Drawings
Fig. 1 is a schematic structural view of the present invention.
Detailed Description
The invention is further illustrated with reference to the following figures and examples.
Taking a blast furnace gas organic sulfur removal test device in the steel industry as an example for explanation, as shown in fig. 1, the system mainly comprises a cooling tower 1, a first gas-liquid contact device 2, an absorption tower 3, a first solvent tank 4, a solvent absorbent tank 5, a first demisting device 6, a first liquid circulating pump 7, a filter 8, a catalyst tank 9, a heat exchanger 10, a second liquid circulating pump 11, a regeneration tower 12, a second gas-liquid contact device 13, a second demisting device 14, a third liquid circulating pump 15, a second solvent tank 16, a steam boiler 17, a cooler 18, a high-speed centrifugal separator 19 and a regenerated acid gas incineration system 20. The cooling tower 1 is arranged at an inlet at the front end of the absorption tower 3, the temperature of the blast furnace gas entering the absorption tower is controlled to be 120-130 ℃, the solvent absorbent of the sulfur dioxide, organic sulfur and hydrogen sulfide in the blast furnace gas in the absorption tower, which is dissolved in the first solvent circulation tank, and the organic acid and the organic amine catalyst (the volume ratio of the organic acid to the organic amine is 2:8) which are added through the first liquid circulation pump 7 form an active intermediate complex, and the active intermediate complex reacts with the tail gas and the hydrogen sulfide dissolved in the solvent to generate elemental sulfur.
After the desulfurization rich solution absorbing blast furnace tail gas is pumped out by a second liquid circulating pump 11 and exchanges heat by a heat exchanger 10 to recover partial heat, the rich solution enters from the top of a regeneration tower 12 and is boiled with steam from bottom to top at a certain temperature of 90-130 ℃ and under the pressure of-50 kpa, stripping steam generated by 17 is in countercurrent contact, and sulfide and CO dissolved in the rich solution are separated out2. The solvent absorbent in the regeneration tower 12 is regenerated to realize recycling, and the partial regeneration of the organic acid and the organic amine catalyst and the recycling of the liquid sulfur are realized in the reaction process.
Dissolved sulfides and CO in the pregnant solution2The lean solution obtained after being resolved enters the absorption tower 3 through a third liquid circulating pump 15 and a third spraying device, so that the recycling of the solvent absorbent is realized. The second liquid circulation pump 11 pumps high-temperature rich liquid from the absorption tower 3 into the heat exchanger 10, the third liquid circulation pump 15 pumps low-temperature lean liquid from the regeneration tower 12 into the heat exchanger 10, the rich liquid and the lean liquid realize heat exchange in the heat exchanger 10, the cooled rich liquid enters the regeneration tower 12, and the heated lean liquid enters the absorption tower 3.
The regenerated acid gas from the top of the regeneration tower is subjected to liquid drop removal by a tower top demisting device, then is conveyed to an acid gas incineration system by a draught fan, and is exhausted into the atmosphere after incineration; and removing liquid drops from the gas in the absorption tower by a tower top demisting device and then discharging the gas into the atmosphere.
Reaction in the absorption column according to H2S/S02The ratio of hydrogen sulfide to sulfur dioxide is 2:1, the solubility of hydrogen sulfide and sulfur dioxide in a solvent is greatly different, and H in a liquid phase is ensured2S/S02The ratio of H to H is 2:1, and the blast furnace tail gas is required to contain H2S/S02The ratio is slightly greater than 2. The main reaction formula is as follows:
organic acid and organic amine solvent catalyst are added into the polyethylene glycol water solution, so that the removal rate of organic sulfur can be improved.
It should be noted that, for those skilled in the art, without departing from the principle of the present invention, several improvements and modifications can be made, and these improvements and modifications should also be construed as the protection scope of the present invention. All the components not specified in the present embodiment can be realized by the prior art.
Claims (8)
1. A blast furnace gas catalytic desulfurization device is characterized by comprising a cooling tower (1), an absorption tower (3), a solvent absorbent tank (5), a catalyst tank (9), a first liquid circulating pump (7) and a filter (8); the air inlet of the cooling tower (1) is connected with blast furnace tail gas, and the air outlet is connected with the air inlet of the absorption tower (3); a first solvent tank (4) is arranged below an air inlet in the absorption tower (3), and a first gas-liquid contact device (2), a first spraying device and a first demisting device (6) are sequentially arranged between the air inlet and an air outlet at the top of the absorption tower (3) from bottom to top; the solvent absorbent tank (5) is communicated with the first solvent tank (4), the catalyst tank (9) and the first solvent tank (4) are both communicated with a liquid inlet of the first liquid circulating pump (7), a liquid outlet of the first liquid circulating pump (7) is connected with a liquid inlet of the filter (8), and a liquid outlet of the filter (8) is connected with the first spraying device; the first solvent tank (4) and the solvent absorbent tank (5) are filled with solvent absorbent for absorbing sulfur dioxide, organic sulfur and hydrogen sulfide in blast furnace gas.
2. The blast furnace gas catalytic desulfurization device according to claim 1, characterized by further comprising a regeneration tower (12), a heat exchanger (10), a second liquid circulation pump (11), a steam boiler (17), a second spray device; a second solvent tank (16) is arranged at the bottom in the regeneration tower (12), and a second demisting device (14) and a second gas-liquid contact device (13) are sequentially arranged between a gas outlet at the top of the regeneration tower (12) and the second solvent tank (16) from top to bottom; the second spraying device is arranged between the demisting device (14) and the second gas-liquid contact device (13); the first solvent tank (4) is connected with a liquid inlet of a second liquid circulating pump (11), a liquid outlet of the second liquid circulating pump (11) is connected with a hot liquid inlet of the heat exchanger (10), and a hot liquid outlet of the heat exchanger (10) is connected with a second spraying device; the liquid inlet of the steam boiler (17) is communicated with the second solvent tank (16), and the steam outlet is arranged between the second gas-liquid contact device (13) and the second solvent tank (16).
3. The catalytic desulfurization device for blast furnace gas according to claim 2, characterized by further comprising a third liquid circulation pump (15), a third spray device; the third spraying device is arranged in the absorption tower (3) and between the first gas-liquid contact device (2) and the first demisting device (6); a liquid inlet of the third liquid circulating pump (15) is communicated with the second solvent tank (16), a liquid outlet is connected with a cold liquid inlet of the heat exchanger (10), and a cold liquid outlet of the heat exchanger (10) is connected with the third spraying device.
4. The catalytic desulfurization apparatus for blast furnace gas according to claim 2, characterized in that the bottom of the second solvent tank (16) is provided with a liquid sulfur discharge port.
5. The blast furnace gas catalytic desulfurization apparatus according to claim 2, characterized by further comprising a cooler (18), a high-speed centrifugal separator (19); the liquid inlet of the cooler (18) is communicated with the second solvent tank (16), the liquid outlet is connected with the high-speed centrifugal separator (19), and the liquid outlet of the high-speed centrifugal separator (19) is connected with the catalyst tank (9).
6. The blast furnace gas catalytic desulfurization device according to claim 2, characterized in that the top outlet of the regeneration tower (12) is connected with an acid gas incineration system.
7. The catalytic desulfurization apparatus for blast furnace gas according to any one of claims 1 to 6, characterized in that the solvent absorbent is a mixture of polyethylene glycol and water, and the catalyst in the catalyst tank (9) is organic acid and organic amine.
8. The blast furnace gas catalytic desulfurization method is characterized by comprising the following steps:
step 1: cooling blast furnace gas by a cooling tower;
step 2: the blast furnace gas enters an absorption tower to contact with a solvent absorbent, sulfur dioxide, organic sulfur and hydrogen sulfide are dissolved in the solvent absorbent, the solvent absorbent reacts with a catalyst to form an active intermediate complex, and the active intermediate complex reacts with the hydrogen sulfide in the solvent absorbent to generate elemental sulfur; circularly pumping the solution at the bottom of the absorption tower into the upper part of the absorption tower;
and step 3: the solution at the bottom of the absorption tower is cooled by a heat exchanger and then is circularly pumped into the upper part of a regeneration tower to be in countercurrent contact with stripping steam generated by a steam boiler from bottom to top, and the dissolved sulfide and CO are separated out2；
And 4, step 4: circularly pumping the solution at the bottom of the regeneration tower into a heat exchanger, exchanging heat with the solution in the absorption tower in the heat exchanger, and then entering the absorption tower;
and 5: circularly pumping the solution at the bottom of the regeneration tower into a cooler, cooling, and then feeding the solution into a high-speed centrifugal separator to separate out a catalyst and a byproduct;
step 6: removing liquid drops of the regenerated acid gas from the top of the regeneration tower through a tower top demisting device, conveying the regenerated acid gas to an acid gas incineration system through a draught fan, and discharging the regenerated acid gas after incineration; and removing liquid drops from the gas in the absorption tower through a tower top demisting device and then discharging the gas.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112521983A (en) * | 2020-09-28 | 2021-03-19 | 福建省气柜设备安装有限公司 | Automatic water replenishing device of gas purification system and control method thereof |
| CN115029163A (en) * | 2022-06-14 | 2022-09-09 | 中琉科技有限公司 | Blast furnace gas sulfur recovery device and system |
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| 四川省石油管理局石油炼制研究所: "大气污染的控制-国外降低克劳斯尾气硫含量的一些方法", 《石油炼制与化工》, no. 1976, pages 55 - 65 * |
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| CN112521983A (en) * | 2020-09-28 | 2021-03-19 | 福建省气柜设备安装有限公司 | Automatic water replenishing device of gas purification system and control method thereof |
| CN115029163A (en) * | 2022-06-14 | 2022-09-09 | 中琉科技有限公司 | Blast furnace gas sulfur recovery device and system |
| CN115029163B (en) * | 2022-06-14 | 2023-03-24 | 中琉科技有限公司 | Blast furnace gas sulfur recovery device and system |
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