CN210826085U - Blast furnace gas catalytic desulfurization device - Google Patents
Blast furnace gas catalytic desulfurization device Download PDFInfo
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- CN210826085U CN210826085U CN201921160761.8U CN201921160761U CN210826085U CN 210826085 U CN210826085 U CN 210826085U CN 201921160761 U CN201921160761 U CN 201921160761U CN 210826085 U CN210826085 U CN 210826085U
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Abstract
The utility model provides a blast furnace gas catalytic desulfurization device, which comprises 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, and the cooled rich solution enters a regeneration towerAnd the heated barren solution enters an 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 utility model relates to a novel catalytic desulfurization device for blast furnace gas, which is applied to the organic sulfur removal of the blast furnace gas in iron and steel plants.
Background
With the three-year action plan of the blue-sky defense war proposed by the department of ecological environment, the air pollution control in the non-electric industry becomes the central importance of the prevention and control of the attack and hardness war, particularly, the emission ratio of pollutants of sintering machines, pellets and blast furnace units in steel plants is large and needs to be firstly controlled, wherein the flue gas conditions of the sintering machines and pellets are similar to the conventional process in the electric power industry, the air pollution control process treatment route can be simply controlled, but the blast furnace gas has no rigid emission index requirements on tail gas due to the self production process and the flue gas conditions, and the environmental protection department does not release the ultra-low emission modification working scheme of steel enterprises, the ultra-low emission modification working scheme of steel enterprises is provided by the environmental protection department, the ultra-low emission modification is completed in the air pollution control areas such as long2： 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.
SUMMERY OF THE UTILITY MODEL
The utility model aims at: 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 for the blast furnace gas, which can stably operate for a long time, is provided.
The technical scheme of the utility model:
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 second 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 second demisting device at the top of the regenerated acid gas tower 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 first demisting device and the second demisting device are multi-channel hook-shaped liquid drop devices which are made of PP plates and used for separating tail gas carried by the liquid drop devices.
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.
The blast furnace gas catalytic desulfurization method based on the utility model 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: the regenerated acid gas coming out of the top of the regeneration tower is subjected to liquid drop removal by a second demisting device at the tower top, then is conveyed to an acid gas incineration system by a draught fan, and is exhausted after incineration; and removing liquid drops of the gas in the absorption tower through a first demisting device at the top of the tower and then discharging the gas.
The utility model discloses beneficial effect: the utility model discloses a design is through precooling tower control tail gas temperature 120-: 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 diagram of the present invention.
Detailed Description
The present invention will be further explained with reference to the drawings 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 barren solution obtained after being analyzed enters a third liquid circulating pump 15 and a third spraying deviceIn the absorption tower 3, 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 coming out of the top of the regeneration tower is subjected to liquid drop removal by a second demisting device at the tower top, 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 through a first demisting device at the top of the tower and then discharging the gas into the atmosphere.
Reaction in the absorption column according to H2S/S022:1, the solubility of hydrogen sulfide and sulfur dioxide in the solvent is very different, in order to ensure H in the liquid phase2S/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 considered 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 (6)
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 second 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.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110591769A (en) * | 2019-07-23 | 2019-12-20 | 南京中电环保科技有限公司 | Blast furnace gas catalytic desulfurization device and method |
| CN112870919A (en) * | 2021-01-04 | 2021-06-01 | 中国神华能源股份有限公司国华电力分公司 | Flue gas CO2Hypergravity regeneration energy-saving process for trapping system |
| CN114276841A (en) * | 2021-12-30 | 2022-04-05 | 新兴铸管股份有限公司 | Desulfurization method of blast furnace gas |
-
2019
- 2019-07-23 CN CN201921160761.8U patent/CN210826085U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110591769A (en) * | 2019-07-23 | 2019-12-20 | 南京中电环保科技有限公司 | Blast furnace gas catalytic desulfurization device and method |
| CN112870919A (en) * | 2021-01-04 | 2021-06-01 | 中国神华能源股份有限公司国华电力分公司 | Flue gas CO2Hypergravity regeneration energy-saving process for trapping system |
| CN114276841A (en) * | 2021-12-30 | 2022-04-05 | 新兴铸管股份有限公司 | Desulfurization method of blast furnace gas |
| CN114276841B (en) * | 2021-12-30 | 2023-10-24 | 新兴铸管股份有限公司 | Desulfurization method for blast furnace gas |
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