CN219898091U - System for preparing sulfuric acid by desulfurizing coke oven gas - Google Patents
System for preparing sulfuric acid by desulfurizing coke oven gas Download PDFInfo
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- CN219898091U CN219898091U CN202320653180.8U CN202320653180U CN219898091U CN 219898091 U CN219898091 U CN 219898091U CN 202320653180 U CN202320653180 U CN 202320653180U CN 219898091 U CN219898091 U CN 219898091U
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 218
- 239000000571 coke Substances 0.000 title claims abstract description 38
- 230000003009 desulfurizing effect Effects 0.000 title claims description 19
- 239000002253 acid Substances 0.000 claims abstract description 245
- 239000007789 gas Substances 0.000 claims abstract description 225
- 238000010521 absorption reaction Methods 0.000 claims abstract description 77
- 238000000034 method Methods 0.000 claims abstract description 55
- 239000002918 waste heat Substances 0.000 claims abstract description 49
- 239000003595 mist Substances 0.000 claims abstract description 29
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 6
- 238000004821 distillation Methods 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 66
- 239000007788 liquid Substances 0.000 claims description 58
- 239000007921 spray Substances 0.000 claims description 21
- 238000004519 manufacturing process Methods 0.000 claims description 13
- 238000003860 storage Methods 0.000 claims description 13
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 7
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 7
- 238000005507 spraying Methods 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 5
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 5
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 5
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 5
- 239000002351 wastewater Substances 0.000 claims description 5
- 238000011010 flushing procedure Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims 1
- 238000006477 desulfuration reaction Methods 0.000 abstract description 17
- 230000023556 desulfurization Effects 0.000 abstract description 17
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 14
- 238000006243 chemical reaction Methods 0.000 abstract description 6
- 230000000694 effects Effects 0.000 abstract description 6
- 238000002360 preparation method Methods 0.000 abstract description 6
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 231100000719 pollutant Toxicity 0.000 abstract description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 8
- 229910000831 Steel Inorganic materials 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 8
- 239000011521 glass Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 8
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 8
- 239000010935 stainless steel Substances 0.000 description 8
- 229910001220 stainless steel Inorganic materials 0.000 description 8
- 239000010959 steel Substances 0.000 description 8
- 239000011449 brick Substances 0.000 description 7
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 229910000975 Carbon steel Inorganic materials 0.000 description 6
- 239000010962 carbon steel Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 239000011152 fibreglass Substances 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 4
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 208000021302 gastroesophageal reflux disease Diseases 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- -1 polyethylene Polymers 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 239000004698 Polyethylene Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 239000010431 corundum Substances 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 description 2
- 229910052863 mullite Inorganic materials 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 229920000573 polyethylene Polymers 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 239000011473 acid brick Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000005465 channeling Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses a sulfuric acid preparation system for desulfurization of coke oven gas, wherein an acid gas inlet of an impact type separator is connected with an acid gas pipeline from an ammonia distillation process, and an acid gas outlet of the impact type separator is connected with an acid gas inlet pipeline of an acid gas fan; the acid gas outlet of the acid gas fan is connected with an acid gas inlet pipeline of the incinerator; the acid gas outlet of the incinerator is connected with an inner heat exchange tube inlet process tube of the waste heat boiler, the inner heat exchange tube outlet of the waste heat boiler is connected with an acid gas inlet at the top of the contact tower, the acid gas outlet at the bottom of the contact tower is connected with an acid gas inlet at the bottom of the absorption tower, and the acid gas outlet at the top of the absorption tower is connected with an acid gas inlet at the bottom of the rod filter. The system realizes the effect of standard emission of tail gas after the desulfurization of the coke oven gas to prepare sulfuric acid, improves the conversion rate of the desulfurization of the coke oven gas to prepare sulfuric acid, reduces the emission of sulfuric acid tail gas pollutants, and realizes the standard limit value of the emission concentration of sulfur dioxide and acid mist in the sulfuric acid tail gas.
Description
Technical Field
The utility model belongs to the technical field of coking chemistry, and particularly relates to a system for preparing sulfuric acid by desulfurizing coke oven gas.
Background
The coke oven gas contains a plurality of chemical components such as ammonia, hydrogen sulfide, hydrogen cyanide, benzene and the like, and after the ammonia, the hydrogen cyanide and the benzene are recovered through purification and absorption, the hydrogen sulfide is required to be recovered and treated to reach the national emission standard. If the hydrogen sulfide is not recycled, precious chemical products are lost, the environment is polluted by external pollution, and serious corrosion of production facilities is easily caused. For this reason, most coking plants adopt wet absorption to produce sulfur process systems; the system has the advantages of complex production process operation, high power consumption and labor intensity, low purity of the prepared sulfur and environmental pollution caused by secondary processing, and is influenced by tar impurities contained in coke oven gas. With the increasing national requirements on environmental protection, the limit value of the emission concentration of sulfur dioxide and acid mist in the tail gas of the coke oven gas desulfurization process must meet the control requirements in GB26132-2010 emission Standard for pollutants for sulfuric acid industry. Therefore, the system is more suitable for preparing sulfuric acid by desulfurizing coke oven gas, realizes the high-efficiency recovery treatment of the coke oven gas desulfurization, and achieves environmental protection and economy win-win effect.
Disclosure of Invention
The utility model aims to solve the technical problem of providing a system for preparing sulfuric acid by desulfurizing coke oven gas, which is used for efficiently recycling and treating the coke oven gas for desulfurization.
In order to solve the technical problems, the utility model adopts the following technical scheme: the device comprises an impact type separator, an incinerator, a waste heat boiler, a contact tower, an absorption tower, a rod type filter, an acid mist filter, a sulfuric acid tail gas absorption tower, a chimney, an acid gas fan and a tail gas fan; the acid gas inlet of the impact type separator is connected with an acid gas pipeline from an ammonia distillation process, and the acid gas outlet of the impact type separator is connected with an acid gas inlet pipeline of an acid gas fan; the acid gas outlet of the acid gas fan is connected with an acid gas inlet pipeline of the incinerator; the acid gas outlet of the incinerator is connected with an inner heat exchange tube inlet process tube of the waste heat boiler, the inner heat exchange tube outlet of the waste heat boiler is connected with an acid gas inlet at the top of the contact tower, an acid gas outlet at the bottom of the contact tower is connected with an acid gas inlet at the bottom of the absorption tower, an acid gas outlet at the top of the absorption tower is connected with an acid gas inlet at the bottom of the rod filter, an acid gas outlet at the top of the rod filter is connected with an acid gas inlet at the bottom of the acid mist filter, an acid gas outlet at the top of the acid mist filter is connected with an acid gas tail gas inlet of the tail gas fan, an acid gas tail gas outlet of the tail gas fan is connected with a tail gas inlet at the bottom of the sulfuric acid tail gas absorption tower, and a tail gas outlet at the top of the sulfuric acid tail gas absorption tower is connected with a bottom inlet of a chimney.
Further, the device also comprises a condensate tank and a condensate pump; the upper ammonia water inlet of the impact type separator is connected with an external circulating ammonia water pipeline, and the bottom flushing liquid outlet of the impact type separator is connected with an inlet pipeline of the condensate tank; an acid vapor condensate outlet of an outlet pipeline of the acid vapor fan is connected with an inlet pipeline of the condensate tank; the outlet of the condensate tank is connected with an inlet process pipeline of a condensate pump, and the outlet of the condensate pump is connected with a gas purifying production system.
Further, the waste heat boiler is also included; the outlet acid steam heat exchange tube of the incinerator is connected with a furnace tube of the waste heat boiler in a closed loop manner, and a shell side of the waste heat boiler is communicated with a softened water pipeline.
Further, the device also comprises a circulating acid pump, a circulating acid tank, a liquid seal tank and a section of sulfuric acid cooler; the top acid liquid spraying pipe of the absorption tower is connected with an outlet pipeline of a circulating acid pump, and an inlet of the circulating acid pump is connected with a bottom outlet process pipeline of the circulating acid tank; the bottom sulfuric acid outlet of the absorption tower is connected with an acid inlet pipe at the top of the liquid seal tank, the bottom outlet of the liquid seal tank is connected with an acid liquid inlet process pipeline of a section of sulfuric acid cooler, and the acid liquid inlet process pipeline of the section of sulfuric acid cooler is connected with the inlet of the circulating acid tank.
Further, the device also comprises a two-stage sulfuric acid cooler, a dilute acid large tank and a dilute acid pump; the inlet of the second-stage sulfuric acid cooler is connected with an outlet process pipeline of the circulating acid pump, the inlet of the dilute acid large tank is connected with an outlet process pipeline of the second-stage sulfuric acid cooler, the outlet of the dilute acid large tank is connected with an inlet process pipeline of the dilute acid pump, and the outlet of the dilute acid pump is connected with an acid process pipeline for an ammonium sulfate process.
Further, the device also comprises an absorption liquid storage tank, a circulating spray pump and a discharge pump; the upper inlet of the absorption liquid storage tank is connected with a bottom absorption liquid outlet process pipeline of the sulfuric acid tail gas absorption tower, the bottom outlet of the absorption liquid storage tank is connected with an inlet process pipeline of the circulating spray pump, and an outlet process pipeline of the circulating spray pump is connected with an upper spray liquid inlet of the sulfuric acid tail gas absorption tower; the bottom emptying port of the absorption liquid storage tank is connected with the inlet of a discharge pump, and the outlet of the discharge pump is connected with a production system process pipeline; the top inlet of the absorption liquid storage tank is connected with an alkali liquor, softened water or wastewater process pipeline.
Furthermore, the top acid gas outlet of the acid mist filter is additionally provided with a path of acid gas outlet which is directly connected with the bottom inlet of the chimney.
The beneficial effects of adopting above-mentioned technical scheme to produce lie in: the utility model adopts the steps of hydrogen sulfide incineration and oxidation in acid steam, heat recovery, catalytic oxidation, wet conversion, condensation and absorption to prepare sulfuric acid, improves the desulfurization conversion rate and reduces the emission of sulfuric acid tail gas sulfur oxide; the sulfuric acid tail gas is subjected to bar filtration and acid mist filtration, so that a large amount of acid liquor in the tail gas can be captured and recovered, and the emission of acid mist is effectively reduced; the acid vapor tail gas is recycled by an alkaline liquid medium spray absorption system, SO that SO in the tail gas after the acid mist filter x The emission concentration limit meets the control requirement in emission standard of sulfuric acid industry pollutant (GB 26132-2010), and simultaneously the tail gas absorption liquid can be comprehensively recycled. The utility model can lead the hydrogen sulfide in the acid vapor to beThe sulfuric acid is prepared by the production process of high-temperature combustion, oxidation reaction, wet absorption and the like, and the residual SO in the sulfuric acid tail gas can be realized x The tail gas is recycled through the tail gas absorption system, so that the effect of standard emission of the tail gas after the sulfuric acid is prepared by the desulfurization of the coke oven gas is achieved, the conversion rate of the sulfuric acid prepared by the desulfurization of the coke oven gas is improved, the pollutant emission of the sulfuric acid tail gas is reduced, the limit value of the emission concentration of sulfur dioxide and acid mist in the sulfuric acid tail gas is reached, the environmental protection benefit is achieved, and the remarkable economic and environmental protection benefits are obtained.
Drawings
The utility model will be described in further detail with reference to the drawings and the detailed description.
Fig. 1 is a schematic structural view of the present utility model.
In the figure: the device comprises an impact type separator 1, an incinerator 2, a waste heat boiler 3, a contact tower 4, an absorption tower 5, a rod type filter 6, an acid mist filter 7, a sulfuric acid tail gas absorption tower 8, a chimney 9, a boiler water supply tank 10, a condensate tank 11, a liquid seal tank 12, a circulating acid tank 13, a dilute acid large tank 14, an absorption liquid storage tank 15, an acid gas fan 16, a gas fan 17, an air fan 18, a tail gas fan 19, a condensate pump 20, a boiler water supply pump 21, a circulating acid pump 22, a dilute acid pump 23, a circulating spray pump 24, a discharge pump 25, a deaerator 26, a throttle cone 27, a primary sulfuric acid cooler 28, a secondary sulfuric acid cooler 29 and a circulating acid reflux sight glass 30.
Detailed Description
As shown in fig. 1, in the sulfuric acid preparation system by desulfurizing coke oven gas, an acid gas inlet of the impact type separator 1 is connected with an acid gas pipeline from an ammonia distillation process, and an acid gas outlet of the impact type separator 1 is connected with an acid gas inlet pipeline of an acid gas fan 16; the acid gas outlet of the acid gas fan 16 is connected with an acid gas inlet pipeline of the incinerator 2; the acid gas outlet of the incinerator 2 is connected with an inner heat exchange tube inlet process tube of the waste heat boiler 3, the inner heat exchange tube outlet of the waste heat boiler 3 is connected with a top acid gas inlet of the contact tower 4, a bottom acid gas outlet of the contact tower 4 is connected with a bottom acid gas inlet of the absorption tower 5, a top acid gas outlet of the absorption tower 5 is connected with a bottom acid gas inlet of the rod filter 6, a top acid gas outlet of the rod filter 6 is connected with a bottom acid gas inlet of the acid mist filter 7, one path of top acid gas outlet of the acid mist filter 7 is connected with an acid gas tail gas inlet of the tail gas fan 19, an acid gas tail gas outlet of the tail gas fan 19 is connected with a bottom tail gas inlet of the sulfuric acid tail gas absorption tower 8, and a top tail gas outlet of the sulfuric acid tail gas absorption tower 8 is connected with a bottom inlet of the chimney 9; the other path of the top acid gas outlet of the acid mist filter 7 is directly connected with the bottom inlet of the chimney 9 and is used as an acid gas tail gas traffic pipeline of the sulfuric acid tail gas absorption tower 8; the top inlet of the chimney 9 is connected to the atmosphere.
In the sulfuric acid preparing system through coke oven gas desulfurization, as shown in fig. 1, an ammonia water inlet at the upper part of an impact type separator 1 is connected with an external circulating ammonia water pipeline, and a flushing liquid outlet at the bottom of the impact type separator 1 is connected with an inlet pipeline of a condensate tank 11; an acid vapor condensate outlet of an outlet pipeline of the acid vapor fan 16 is connected with an inlet pipeline of the condensate tank 11; the outlet of the condensate tank 11 is connected with an inlet process pipeline of the condensate pump 20, and the outlet of the condensate pump 20 is connected with a gas purifying production system.
In the system for preparing sulfuric acid by desulfurizing coke oven gas, as shown in fig. 1, the inlet of the incinerator 2 is respectively connected with outlet process pipelines of an acid gas fan 16, a gas fan 17 and an air fan 18; wherein the inlet of the gas fan 17 is connected with a coke oven gas pipe network, and the inlet of the air fan 18 is connected with the atmosphere.
As shown in fig. 1, in the sulfuric acid production system by coke oven gas desulfurization, an upper water inlet of the waste heat boiler 3 is connected with an outlet of a boiler water feeding pump 21, an inlet of the boiler water feeding pump 21 is connected with a softened water outlet at the bottom of a boiler water feeding tank 10, the top of the boiler water feeding tank 10 is connected with a deaerator 26, an upper water inlet of the deaerator 26 is connected with a softened water process pipeline, and a steam inlet pipe of a steam distributor at the bottom of the boiler water feeding tank 10 is connected with a steam pipe network; the top steam outlet of the waste heat boiler 3 is connected with a steam pipe network for coking production; the top of the waste heat boiler 3 is provided with a safety relief valve and a manual relief valve which are used as pressure relief facilities of the waste heat boiler 3; the upper furnace tube and the lower furnace tube at the bottom of the waste heat boiler 3 are connected with an acid steam heat exchange tube at the outlet of the incinerator 2, and are used for exchanging heat with high Wen Suanqi as softened water in the waste heat boiler 3, so that the temperature of the acid steam is reduced, and meanwhile, medium-pressure steam is produced, so that the waste heat utilization and energy conservation effects are achieved.
In the sulfuric acid preparing system through the coke oven gas desulfurization, as shown in fig. 1, the inner diameter side of the central tube of the acid steam heat exchange tube bundle of the waste heat boiler 3 is contacted with the outer diameter side of the throttling cone 27, and the throttling cone 27 is adjusted to enable the central tube of the acid steam heat exchange tube bundle of the waste heat boiler 3 to be in a blocking and opening state, so that the heat exchange quantity between the post-height Wen Suanqi of the incinerator 2 and softened water in the waste heat boiler 3 is achieved, and the temperature of the acid steam entering the contact tower 4 is regulated and controlled to reach the standard.
As shown in figure 1, in the sulfuric acid preparing system by desulfurizing coke oven gas, a plurality of layers of grating catalysts are arranged in the contact tower 4, and each layer of catalyst grating layer is connected with an air inlet pipeline of an air blower 18 and is used as a catalyst catalytic bed for the oxidation reaction of high-temperature acid gas and air.
In the sulfuric acid preparation system through coke oven gas desulfurization, as shown in fig. 1, an acid gas inlet at the bottom of an absorption tower 5 is connected with an acid gas pipeline from a contact tower 4, an acid liquid spraying pipe at the top of the absorption tower 5 is connected with an outlet pipeline of a circulating acid pump 22, and an inlet of the circulating acid pump 22 is connected with a bottom outlet process pipeline of a circulating acid tank 13; the bottom sulfuric acid outlet of the absorption tower 5 is connected with the top acid inlet pipe of the liquid seal tank 12, the bottom outlet of the liquid seal tank 12 is connected with the acid liquor inlet process pipeline of the first section sulfuric acid cooler 28 through a circulating acid reflux sight glass 30, and the acid liquor inlet process pipeline of the first section sulfuric acid cooler 28 is connected with the inlet of the circulating acid tank 13.
As shown in figure 1, in the sulfuric acid preparation system for the coke oven gas desulfurization, the inlet of the dilute acid large tank 14 is connected with the outlet process pipeline of the second-stage sulfuric acid cooler 29, the inlet of the second-stage sulfuric acid cooler 29 is connected with the outlet process pipeline of the circulating acid pump 22, the outlet of the dilute acid large tank 14 is connected with the inlet process pipeline of the dilute acid pump 23, and the outlet of the dilute acid pump 23 is connected with the acid process pipeline for the ammonium sulfate working procedure.
As shown in FIG. 1, the technological process of preparing sulfuric acid by adopting the coke oven gas desulfurization system comprises the following steps:
the rich liquid produced by purifying and washing coke oven gas through a desulfurization process is deacidifiedThe H2S-containing acid gas generated in the working procedure enters from bottom to top from the lower part of the impact type separator 1 and is separated into partial acid liquid through the grid layer; the acid liquor automatically flows to a condensate tank 11 through a liquid discharge pipe at the bottom of the impact type separator 1, and a liquid medium in the condensate tank 11 is conveyed to a gas purifying production system by a condensate pump 20; the top of the impact separator 1 separates acid gas, which is pumped to the incinerator 2 by an acid gas fan 16 and O in the air blown by an air fan 18 2 The combustion temperature reaches 900-1080 ℃, and oxidation-reduction reaction is carried out in the incinerator 2 to generate SO 2 The method comprises the steps of carrying out a first treatment on the surface of the After the softened water is deoxidized by a deaerator 26 at the top of a boiler water supply tank 10, the softened water is pumped into a heat exchange pipe of a waste heat boiler 3 by a boiler water supply pump 21 to exchange heat with the high Wen Suanqi from the incinerator 2, the temperature of the acid steam at 950-1080 ℃ is reduced to 430-470 ℃ by adjusting a throttling cone 27 at the rear part of the waste heat boiler 3, the top of a contact tower 4 passes through various layers of grid catalyst catalysts from top to bottom, and the softened water and air blown in by an air blower 18 undergo oxidation reaction within the range of 450+/-10 ℃ to generate SO 3 The method comprises the steps of carrying out a first treatment on the surface of the SO-containing at 410+ -10deg.C from the bottom of the contact column 4 3 The acid gas enters from bottom to top of the absorption tower 5, and reacts with dilute acid (or water) sprayed from the top of the absorption tower 5 in countercurrent contact to generate H 2 SO 4 The waste water enters the liquid seal tank 12 automatically from the bottom of the absorption tower 5, is cooled to 25-40 ℃ through a full flow pipe of the liquid seal tank 12 by a section of sulfuric acid cooler 28, enters the circulating acid tank 13, is conveyed by the circulating acid pump 22, one part of the waste water enters a spray pipe at the top of the absorption tower 5 to absorb SO3 in acid steam, and the other part of the waste water enters the dilute acid tank 14 through a second section of sulfuric acid cooler 29, and is conveyed to an ammonium sulfate working procedure by the dilute acid pump 23 to be used as raw material acid for producing ammonium sulfate products. The acid gas at the upper part of the absorption tower 5 enters from the top of the rod filter 6, after passing through the rod filter 6 and filtering the rod filter, enters from the bottom of the rod filter 6 into the bottom of the acid mist filter 7, and after acid mist is captured by the filtering device from bottom to top, the acid gas is pumped to the bottom of the sulfuric acid tail gas absorption tower 8 from the top of the acid mist filter 7 through the tail gas fan 19, the acid gas passes through the packing in the sulfuric acid tail gas absorption tower 8 from bottom to top, and SO in the alkaline liquid sprayed by the upper part of the sulfuric acid tail gas absorption tower 8 is absorbed by the alkali liquid sprayed by the upper part of the sulfuric acid tail gas absorption tower 8 x Then discharged into a chimney 9, the absorption liquid at the bottom of the sulfuric acid tail gas absorption tower 8 flows into an absorption liquid storage tank 15 from the bottom, and part of the absorption liquid is sent to the sulfuric acid tail gas absorption tower 8 to be sprayed by a circulating spray pump 24The sulfuric acid tail gas is absorbed, and the other part is conveyed to the production system for digestion treatment by a discharge pump 25.
As shown in FIG. 1, the start-up and shutdown of the system for preparing sulfuric acid by desulfurizing coke oven gas are carried out by the following steps:
a. sulfuric acid start-up operation:
(1) Checking and confirming that the external condition of the sulfuric acid system is good, and the ignition program accords with the condition;
(2) Closing the throttle cone 27 of the outlet of the waste heat boiler 3;
(3) Checking the water levels of the waste heat boiler 3 and the boiler water supply tank 10, and putting the boiler water supply pump 21 into operation;
(4) After the air blower 18 is started, the gas blower 17 is started;
(5) The gas of the ignition burner of the incinerator 2 is opened and ignited;
(6) Adjusting the gas quantity at the outlet of the gas fan 17 and the temperature of the hearth in the incinerator 2 according to the temperature rising curve;
(7) When the temperature of the incinerator 2 reaches above 600 ℃, opening a throttling cone 27 at the outlet of the waste heat boiler 3 to enable the temperature of the outlet of the waste heat boiler 3 to be higher than 350 ℃;
(8) Stopping heating when the furnace temperature of the incinerator 2 reaches more than 800 ℃, and then plugging a triangular cover in front of the contact tower 4;
(9) The incinerator 2 is heated again, and the throttle cone 27 is regulated, so that the temperature of the flue gas at the outlet of the waste heat boiler 3 reaches about 450 ℃;
(10) Turning on the circulating acid pump 22 and adjusting the outlet flow to the reflux sight glass to show full flow;
(11) The first-stage sulfuric acid cooler 28 and the second-stage sulfuric acid cooler 29 are led into cooling water for operation;
(12) The acid gas fan 16 is started, and the acid gas pipeline is used for discharging sewage. Acid gas is sent into the incinerator 2, and the gas blower 17 is started and stopped according to the temperature of the incinerator 2 to output gas auxiliary burner.
b. Operation of waste heat boiler 3:
(1) Deoxygenated water is filled into the waste heat boiler 3, the temperature is generally not higher than 100 ℃, water is slowly filled when the temperature of the incinerator 2 is low, and the water is added into the boiler until the water level reaches the upper cylinder;
(2) In the water feeding process, checking whether the pressure-bearing members of the waste heat boiler 3 leak or not, and finding that the leakage stops water feeding and processing;
(3) During the start-up boost process, all the auxiliary equipment and detection devices, in particular the waste heat boiler 3 water level indication, water supply and discharge devices, safety valves, pressure gauges etc. are checked and confirmed to be good. The indirect water level indicator should be consistent with the direct water level indicator;
(4) In the preheating process, a diffusing pipe of the waste heat boiler 3 is opened until steam overflows;
(5) The throttle cone 27 at the outlet of the waste heat boiler 3 is adjusted so that the steam pressure at which the temperature rises after heat exchange between the high Wen Suanqi and the softened water in the waste heat boiler 3 is in accordance with the technical specifications.
c. Operation of starting the boiler water supply tank 10:
(1) Opening a water inlet valve of a water feeding tank 10 of the boiler to feed water;
(2) Slightly opening an exhaust valve at the top of the boiler water supply tank 10;
(3) Opening a steam valve of a boiler water supply tank 10 to supply steam for heating;
(4) Checking the temperature, pressure and water level of the water supply tank. When the water level is normal and the water temperature reaches 102-104 ℃, water can be sent to the waste heat boiler 3;
(5) When water is required to be continuously supplied to the boiler water supply tank 10 and the water supply amount is required to be adjusted to increase or decrease, the sudden increase or sudden decrease of the pressure of the deaerator 26 at the top of the boiler water supply tank 10 is prevented, and the deaeration effect is prevented from being affected.
The shutdown of the system for preparing sulfuric acid by desulfurizing coke oven gas is carried out by the following steps:
d. sulfuric acid shutdown operation:
(1) The air blower 1 and the gas blower 17 are stopped only after a short time of stopping;
(2) If the machine is stopped for a long time, the following work is performed:
(1) stopping the air blower 1 and the gas blower 17;
(2) the sulfuric acid of the circulating acid tank 13 is sent to a dilute acid large tank 14 until the liquid level reaches 10%, and the circulating acid pump 22 is stopped;
(3) cooling water of the primary sulfuric acid cooler 28 and the secondary sulfuric acid cooler 29 is stopped;
(4) opening an acid gas bypass of a raw gas pipeline before the primary cooler, and stopping an acid gas fan 16;
(5) removing three-way angle covers in front of the contact tower 4 and in front of the absorption tower 5;
(6) after the temperature of the incinerator 2 is reduced to normal temperature, the boiler feed pump 21 is stopped, and the boiler feed water tank 10 is stopped.
e. Shutdown of the boiler feed water tank 10:
(1) Closing a steam valve to the boiler feed water tank 10;
(2) Closing a water feed valve to the boiler water feed tank 10;
(3) When the water bottle is stopped for a long time, the water is discharged.
As shown in fig. 1, the sulfuric acid preparing system for the desulfurization of coke oven gas adopts the following steps:
f. the concentration of sulfuric acid is low:
(1) Reducing the cooling temperature of the acid gas entering the incinerator 2;
(2) Reducing the amount of coal gas entering the incinerator 2;
(3) Regulating and controlling the acid amount in the incinerator 2 and confirming the normal state;
(4) Regulating and controlling the temperature of each layer of acid gas of the contact tower 4 to be in accordance with 450+/-10 ℃;
(5) Adjusting the impact separator 1, and keeping the liquid discharge smooth by the acid gas fan 16 liquid discharge system;
(6) If necessary, the concentrated acid is supplemented to ensure the concentration of sulfuric acid.
g. The waste heat boiler 3 has low steam pressure:
(1) The outlet temperature of the waste heat boiler 3 is lower, a throttling cone 27 at the outlet of the waste heat boiler 3 is regulated, and the outlet temperature is increased to 470 ℃;
(2) The steam valve, the water feed valve, and the drain valve of the waste heat boiler 3 were inspected and confirmed strictly.
h. Sulfuric acid system resistance is high:
(1) Checking the liquid discharge pipes of the rod filter 6 and the acid mist filter 7 to ensure smooth liquid discharge;
(2) The resistance of the rod filter 6 and the acid mist filter 7 was checked and confirmed, and when the resistance was high, the filter rod or the acid mist filter element was replaced.
i. The temperature of the exhaust gas after the absorption tower 5 is high:
(1) Checking the effect of the first-stage sulfuric acid cooler 28, wherein the temperature of the circulating acid is 20-40 ℃, and if the circulating acid is high, the cooling water quantity of the first-stage sulfuric acid cooler 28 is increased;
(2) Checking and confirming whether the spray head at the top of the absorption tower 5 falls off, and if so, replacing the spray head;
(3) Checking the flow of the circulating acid reflux sight glass 30, if the flow is small, opening the outlet valve of the large circulating acid pump 22, and pouring the circulating acid pump 22 for later use if necessary.
The tail gas absorption spray tower of the sulfuric acid preparation system by desulfurizing coke oven gas uses novel absorption filler, adopts a branch pipe type spray device, and is provided with a polyethylene net defogging filter at the top; alkali liquor is pumped to each spraying device in the tower through a circulating pump, the whole section of the tower body is covered completely, and the alkali liquor is fully contacted with tail gas from bottom to top in a countercurrent manner to complete the mass transfer process, so that the tail gas purifying purpose is achieved. Tail gas and alkaline aqueous solution (containing NH) in spray tower 3 Or NaOH) is fully contacted, and sulfuric acid mist and sulfur dioxide gas are reacted and neutralized to generate the catalyst containing (NH) 4 ) 2 SO 4 、(NH 4 ) 2 SO 3 (or Na 2 SO 4 And Na (Na) 2 SO 3 ) Is discharged to a production system for digestion and absorption; and the trace water mist, sulfuric acid mist and sulfur dioxide pass through a mist filtering device at the top of the spray tower and are finally discharged through a chimney, so that the national environment-friendly discharge requirement is met.
One specific example of the sulfuric acid preparation system by desulfurizing coke oven gas is as follows:
the impact type separator 1 is characterized in that a separator body with the diameter of 900mm, the height of 5458mm and the wall thickness of 10mm is selected, an acid gas inlet at the lower part of the separator body is made of stainless steel with the diameter of 300mm and the wall thickness of 10mm, an acid gas outlet at the top of the separator body is made of stainless steel with the diameter of 300mm and the wall thickness of 10mm, an ammonia water inlet at the upper part of the separator body is made of stainless steel with the diameter of 50mm and the wall thickness of 5mm, and a flushing liquid outlet at the bottom of the separator body is made of stainless steel with the diameter of 80mm and the wall thickness of 5 mm.
The incinerator 2 adopts a horizontal body with a variable diameter of 2280/2200mm, a length of 5638mm and a wall thickness of 10 mm; is one of the main devices for producing sulfuric acid by utilizing acid vapor, and generates sulfur dioxide by the reaction of hydrogen sulfide in an incinerator. The acid gas inlet of the front hearth of the incinerator 2 is a connector with the diameter of 300mm and the wall thickness of 10mm, the air inlet is a connector with the diameter of 200mm and the wall thickness of 8mm, and the gas inlet is a connector with the diameter of 50mm and the wall thickness of 5 mm; the incinerator 2 selects the operating pressure of 0.02MPa and the operating temperature of 1100 ℃ (hearth)/350 ℃ (furnace wall); the burner of the main part of the incinerator 2 adopts a high-strength premixed combustion technology, so that the automatic ignition of an ignition gun is realized, the ignition operation intensity is reduced, and the ignition success rate is improved; and a flame real-time monitoring control system is provided. The inner lining of the incinerator 2 adopts a large brick structure with mortises, so that straight seams of refractory bricks on a fire-facing layer are avoided, acid gas channeling is prevented, and accumulated cracks caused by shrinkage of brick seams at high temperature are eliminated; the mortises are coated with high-temperature-resistant and corrosion-resistant special cement, and each brick is bonded into a whole by the cement at high temperature, so that the possibility of corrosion caused by high-temperature gas entering the steel shell in a stringing way is avoided, and the service life of the incinerator 2 is effectively prolonged. The lining of the incinerator 2 is divided into three layers: the first layer adopts a fire-facing layer (refractory layer) of a special corundum mullite brick, and the second layer adopts a refractory heat-insulating layer of a light mullite brick with better temperature resistance; the third layer adopts a light heat-insulating casting material with higher strength.
The waste heat boiler 3 is used for recovering reaction heat generated when hydrogen sulfide reacts in the incinerator 1 to generate sulfur dioxide, and is a natural circulation fire tube type waste heat boiler which is divided into an upper boiler barrel, a lower boiler barrel, a front smoke box and a rear smoke box, wherein the working pressure is 4.4MPa, the rated steam flow is 3.6t/h, the rated steam temperature is 256 ℃, the acid steam inlet temperature is 1150-1200 ℃, and the acid steam outlet temperature is 550-600 ℃. The upper drum is a steam drum and is connected with the lower drum through a rising pipe, wherein the rising pipe is used as a support of the steam drum at the same time; the steam drum is internally provided with a steam-water separator, and is formed by rolling and welding steel plates; an evaporation heating surface (fire tube) is arranged in the lower boiler barrel. The tube plate adopts a flexible tube plate, the furnace gas side of the front tube plate is protected by special heat-resistant concrete, and the furnace gas inlet end of the fire tube is provided with a high-strength heat-resistant heat-insulating corundum sleeve, so that the tube plate is not subjected to or bears small temperature difference stress; the lower part of the boiler barrel is provided with a periodic blow-down pipe; the boiler barrel is formed by adopting steel plate coil welding; the lower boiler barrel is provided with a central pipe throttling cone 27, the material of which is mainly Cr25Ni20, and is used for adjusting the exhaust temperature of the waste heat boiler 3 and ensuring that the acid gas entering the absorption tower 5 meets the process requirements; the front smoke box and the rear smoke box are provided with manholes for overhauling and ash cleaning; the lower boiler barrel is provided with two supports, wherein the inlet end of the boiler gas is a sliding support, and the other is a fixed support. The bottom of the sliding support adopts a polytetrafluoroethylene plate as a supporting pad, so that the friction coefficient is small, and the thermal expansion of the furnace body is facilitated.
The contact tower 4 is made of carbon steel with the diameter of 3000mm and the height of 9100mm, acid-resistant and high-temperature-resistant bricks are lined, 4 layers of grids filled with catalyst are arranged in the cavity, an acid steam inlet at the top of the tower body is an interface with the diameter of 800mm and the wall thickness of 12mm, an acid steam outlet at the bottom of the tower body is an interface with the diameter of 800mm and the wall thickness of 12mm, and an air inlet at the side of the grid filled with the catalyst is an interface with the diameter of 200mm and the wall thickness of 5 mm.
The absorption tower 5 is a carbon steel tank body with the diameter of 3400mm, the height of 8500mm and a lead plate lining a cylinder body, the acid gas inlet at the bottom is an interface with the diameter of 800mm and the wall thickness of 12mm, the acid gas outlet at the upper is an interface with the diameter of 800mm and the wall thickness of 12mm, and the acid liquid spraying port at the top is an interface with the diameter of 200mm and the wall thickness of 10 mm; an acid-resistant grille is arranged at the upper edge of the acid steam inlet at the bottom, and ceramic ring fillers are uniformly arranged on the grille.
The rod filter 6 is a carbon steel semicircle with the diameter of 1500mm, the height of 1950mm and a lead plate lining the cylinder, the top acid steam inlet is an interface with the diameter of 800mm and the wall thickness of 12mm, the lower acid steam outlet is an interface with the diameter of 800mm and the wall thickness of 12mm, and the upper edge of the bottom acid steam inlet is welded with a distribution plate provided with a plurality of filter rods.
The acid mist filter 7 is an acid-resistant tank body with the diameter of 2200mm and the height of 5000mm, the acid steam inlet at the bottom is an interface with the diameter of 800mm and the wall thickness of 12mm, the acid steam outlet at the top is an interface with the diameter of 800mm and the wall thickness of 12mm, and the upper part of the inner side of the cylinder body is provided with a supporting frame of 4 filter cotton stick bodies.
The sulfuric acid tail gas absorption tower 8 is a tank body with a diameter of 2000mm and a height of 8800mm and made of 304 materials, a cylinder body is filled with multi-surface hollow ball filler, and a demisting filter made of a polyethylene net is arranged at the top of the cylinder body; the acid gas inlet at the lower part of the tower adopts an interface with the diameter of 800mm and the wall thickness of 12mm, the acid gas outlet at the top of the tower adopts an interface with the diameter of 800mm and the wall thickness of 12mm, and the spray liquid inlet at the upper part of the tower adopts an interface with the diameter of 100mm and the wall thickness of 5 mm.
The chimney 9 is a cylinder with the diameter of 1400mm/600mm and the height of 40450 mm.
The boiler water supply tank 10 is a horizontal tank body with the diameter of 1500mm and the length of 3400mm, the top is provided with a deaerator 26 with the diameter of 500mm and the length of 1500mm, a softened water inlet is a joint with the diameter of 50mm and the wall thickness of 4mm, a steam inlet is a joint with the diameter of 80mm and the wall thickness of 6mm, and a softened water outlet at the bottom is a joint with the diameter of 80mm and the wall thickness of 6 mm.
The condensate tank 11 is a cylinder with the diameter of 3400mm and the height of 2825mm, the condensate inlet is made of stainless steel with the diameter of 80mm and the wall thickness of 5mm, and the condensate outlet is made of stainless steel with the diameter of 80mm and the wall thickness of 5 mm.
The liquid seal tank 12 is a carbon steel cylinder with an acid-resistant brick lining, wherein the diameter of the carbon steel cylinder is 800mm, the height of the carbon steel cylinder is 2500mm, the diameter of the glass steel pipe lining is 250mm, the wall thickness of the glass steel pipe lining is 10mm, and the diameter of the glass steel pipe lining is 250mm, and the wall thickness of the glass steel pipe lining is 10 mm.
The circulating acid tank 13 is an acid-resistant tank body with the diameter of 2200mm and the height of 2500mm, the sulfuric acid inlet is a lining glass fiber reinforced plastic pipe with the diameter of 250mm and the wall thickness of 10mm, and the sulfuric acid outlet is a lining glass fiber reinforced plastic pipe with the diameter of 200mm and the wall thickness of 10 mm.
The dilute acid large tank 14 is a glass fiber reinforced plastic tank body with the diameter of 4000mm and the height of 8640mm, the sulfuric acid inlet is a lining glass fiber reinforced plastic pipe with the diameter of 80mm and the wall thickness of 8mm, and the sulfuric acid outlet is a lining glass fiber reinforced plastic pipe with the diameter of 50mm and the wall thickness of 5 mm.
The absorption liquid storage tank 15 is a steel lining rubber box body with the length of 3000mm, the width of 3000mm and the height of 2000mm, the absorption liquid outlet is a stainless steel pipe with the diameter of 100mm and the wall thickness of 5mm, and the spraying liquid inlet is a stainless steel pipe with the diameter of 100mm and the wall thickness of 5 mm.
The acid gas fan 16 is selected from specification q=1400 m 3 And/h, motor power 37KW.
The gas fan 17 is selected from specification g=2.68m 3 /min, the motor power is 2.2KW.
The air blower 18 is selected from the specification C150-1.2/0.95.
The tail gas fan 19 is selected from the specification q=6000 m 3 /h、P=5000Pa。
The condensate pump 20 is a motor model MCZ32-160, with specification q=10m3/H, h=32m, and material SS316L.
The boiler feed water pump 21 is selected from motor models MC40-14, P=37KW and specification Q=6m 3 /h、H=567m。
The circulating acid pump 22 is a motor model CMF100-80-180F, N =30kw, and the specification q=100deg.M 3 and/H, H=37m, and the material is lined with tetrafluoro.
The dilute acid pump 23 is a motor model CMF65-40-200F, N =11kw, and the specification q=24m 3 and/H, H=50m, and the material is lined with tetrafluoro.
The circulating spray pump 24 adopts 65FHB-54-B, Q =50m 3 /h，H=38m，N=15KW。
The discharge pump 25 is selected from the specifications of 50FHB-30 and Q=15m 3 /h、H=21m、N=4KW。
The primary sulfuric acid cooler 28 adopts a heat exchange area F=225 m 2 L=5730, 9 groups of spray lead tube heat exchangers.
The heat exchange area F=6m of the two-stage sulfuric acid cooler 29 is selected 2 L=5730.
Claims (7)
1. A sulfuric acid preparing system for desulfurizing coke oven gas is characterized in that: the device comprises an impact type separator (1), an incinerator (2), a waste heat boiler (3), a contact tower (4), an absorption tower (5), a rod type filter (6), an acid mist filter (7), a sulfuric acid tail gas absorption tower (8), a chimney (9), an acid gas fan (16) and a tail gas fan (19); an acid gas inlet of the impact type separator (1) is connected with an acid gas pipeline from an ammonia distillation process, and an acid gas outlet of the impact type separator (1) is connected with an acid gas inlet pipeline of an acid gas fan (16); an acid gas outlet of the acid gas fan (16) is connected with an acid gas inlet pipeline of the incinerator (2); the acid steam outlet of the incinerator (2) is connected with an inner heat exchange tube inlet process tube of the waste heat boiler (3), the inner heat exchange tube outlet of the waste heat boiler (3) is connected with an acid steam inlet at the top of the contact tower (4), the acid steam outlet at the bottom of the contact tower (4) is connected with an acid steam inlet at the bottom of the absorption tower (5), the acid steam outlet at the top of the absorption tower (5) is connected with an acid steam inlet at the bottom of the rod filter (6), the acid steam outlet at the top of the rod filter (6) is connected with an acid steam inlet at the bottom of the acid mist filter (7), the acid steam outlet at the top of the acid mist filter (7) is connected with an acid steam tail gas inlet of the tail gas fan (19), the acid steam tail gas outlet of the tail gas fan (19) is connected with a tail gas inlet at the bottom of the sulfuric acid tail gas absorption tower (8), and the tail gas outlet at the top of the sulfuric acid tail gas absorption tower (8) is connected with a bottom inlet of the chimney (9).
2. A system for preparing sulfuric acid by desulfurizing coke oven gas according to claim 1, characterized in that: the device also comprises a condensate tank (11) and a condensate pump (20); the upper ammonia water inlet of the impact type separator (1) is connected with an external circulating ammonia water pipeline, and the bottom flushing fluid outlet of the impact type separator (1) is connected with an inlet pipeline of a condensate tank (11); an acid vapor condensate outlet of an outlet pipeline of the acid vapor fan (16) is connected with an inlet pipeline of the condensate tank (11); the outlet of the condensate tank (11) is connected with an inlet process pipeline of the condensate pump (20), and the outlet of the condensate pump (20) is connected with the gas purifying production system.
3. A system for preparing sulfuric acid by desulfurizing coke oven gas according to claim 1, characterized in that: also comprises a waste heat boiler (3); the outlet acid steam heat exchange tube of the incinerator (2) is connected with the furnace tube of the waste heat boiler (3) in a closed loop manner, and a softening water pipeline is communicated with the shell side of the waste heat boiler (3).
4. A system for preparing sulfuric acid by desulfurizing coke oven gas according to claim 1, characterized in that: the device also comprises a circulating acid pump (22), a circulating acid tank (13), a liquid seal tank (12) and a section of sulfuric acid cooler (28); the top acid liquid spraying pipe of the absorption tower (5) is connected with an outlet pipeline of the circulating acid pump (22), and an inlet of the circulating acid pump (22) is connected with a bottom outlet process pipeline of the circulating acid tank (13); the bottom sulfuric acid outlet of the absorption tower (5) is connected with an acid inlet pipe at the top of the liquid seal tank (12), the bottom outlet of the liquid seal tank (12) is connected with an acid liquid inlet process pipeline of a section of sulfuric acid cooler (28), and an acid liquid inlet process pipeline of the section of sulfuric acid cooler (28) is connected with the inlet of the circulating acid tank (13).
5. The system for preparing sulfuric acid by desulfurizing coke oven gas according to claim 4, characterized in that: the device also comprises a two-stage sulfuric acid cooler (29), a dilute acid large tank (14) and a dilute acid pump (23); the inlet of the second-stage sulfuric acid cooler (29) is connected with an outlet process pipeline of the circulating acid pump (22), the inlet of the dilute acid large tank (14) is connected with an outlet process pipeline of the second-stage sulfuric acid cooler (29), the outlet of the dilute acid large tank (14) is connected with an inlet process pipeline of the dilute acid pump (23), and the outlet of the dilute acid pump (23) is connected with an acid process pipeline for an ammonium sulfate process.
6. A system for preparing sulfuric acid by desulfurizing coke oven gas according to claim 1, characterized in that: the device also comprises an absorption liquid storage tank (15), a circulating spray pump (24) and a discharge pump (25); the upper inlet of the absorption liquid storage tank (15) is connected with a bottom absorption liquid outlet process pipeline of the sulfuric acid tail gas absorption tower (8), the bottom outlet of the absorption liquid storage tank (15) is connected with an inlet process pipeline of the circulating spray pump (24), and the outlet process pipeline of the circulating spray pump (24) is connected with an upper spray liquid inlet of the sulfuric acid tail gas absorption tower (8); the bottom vent of the absorption liquid storage tank (15) is connected with the inlet of the discharge pump (25), and the outlet of the discharge pump (25) is connected with the process pipeline of the production system; the top inlet of the absorption liquid storage tank (15) is connected with an alkali liquor, softened water or wastewater process pipeline.
7. A system for preparing sulfuric acid by desulfurizing coke oven gas according to any one of claims 1 to 6, characterized in that: the top acid gas outlet of the acid mist filter (7) is additionally provided with a path of acid gas outlet which is directly connected with the bottom inlet of the chimney (9).
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