CN111232934A - Device for utilizing desulfurization waste liquid and operation method thereof - Google Patents
Device for utilizing desulfurization waste liquid and operation method thereof Download PDFInfo
- Publication number
- CN111232934A CN111232934A CN202010195400.8A CN202010195400A CN111232934A CN 111232934 A CN111232934 A CN 111232934A CN 202010195400 A CN202010195400 A CN 202010195400A CN 111232934 A CN111232934 A CN 111232934A
- Authority
- CN
- China
- Prior art keywords
- acid
- gas
- tower
- section
- enters
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000007788 liquid Substances 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 64
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 62
- 230000023556 desulfurization Effects 0.000 title claims abstract description 62
- 239000002699 waste material Substances 0.000 title claims abstract description 34
- 238000010521 absorption reaction Methods 0.000 claims abstract description 78
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 69
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 59
- 239000011593 sulfur Substances 0.000 claims abstract description 56
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 56
- 238000006243 chemical reaction Methods 0.000 claims abstract description 50
- 230000008569 process Effects 0.000 claims abstract description 44
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 37
- 230000004087 circulation Effects 0.000 claims abstract description 22
- 238000004939 coking Methods 0.000 claims abstract description 15
- 239000003054 catalyst Substances 0.000 claims abstract description 12
- 230000003197 catalytic effect Effects 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 154
- 239000002253 acid Substances 0.000 claims description 89
- 238000001035 drying Methods 0.000 claims description 51
- 238000001816 cooling Methods 0.000 claims description 36
- 238000005406 washing Methods 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- 239000002002 slurry Substances 0.000 claims description 17
- 229910001220 stainless steel Inorganic materials 0.000 claims description 17
- 239000010935 stainless steel Substances 0.000 claims description 17
- 238000003860 storage Methods 0.000 claims description 14
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 9
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 9
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 9
- 239000000047 product Substances 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 8
- 229920006395 saturated elastomer Polymers 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 7
- 238000000746 purification Methods 0.000 claims description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 6
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 6
- 239000003595 mist Substances 0.000 claims description 6
- 239000008247 solid mixture Substances 0.000 claims description 6
- 238000007872 degassing Methods 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 5
- 229910052593 corundum Inorganic materials 0.000 claims description 4
- 239000010431 corundum Substances 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 239000005864 Sulphur Substances 0.000 claims description 3
- 230000001276 controlling effect Effects 0.000 claims description 3
- 239000011152 fibreglass Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000007711 solidification Methods 0.000 claims description 3
- 230000008023 solidification Effects 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- 239000006096 absorbing agent Substances 0.000 claims description 2
- 238000006555 catalytic reaction Methods 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000005485 electric heating Methods 0.000 claims description 2
- 238000012423 maintenance Methods 0.000 claims description 2
- 238000012544 monitoring process Methods 0.000 claims description 2
- 239000002245 particle Substances 0.000 claims description 2
- 238000003756 stirring Methods 0.000 claims description 2
- 239000013589 supplement Substances 0.000 claims description 2
- 239000002912 waste gas Substances 0.000 claims description 2
- 239000002918 waste heat Substances 0.000 claims description 2
- 239000000945 filler Substances 0.000 claims 1
- 239000007921 spray Substances 0.000 claims 1
- 239000006260 foam Substances 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000000835 fiber Substances 0.000 abstract description 4
- 239000000853 adhesive Substances 0.000 abstract description 2
- 230000001070 adhesive effect Effects 0.000 abstract description 2
- 239000000919 ceramic Substances 0.000 abstract description 2
- 239000011248 coating agent Substances 0.000 abstract description 2
- 238000000576 coating method Methods 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000011094 fiberboard Substances 0.000 abstract description 2
- 230000009467 reduction Effects 0.000 abstract description 2
- 229910052720 vanadium Inorganic materials 0.000 abstract description 2
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 abstract description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- ZMZDMBWJUHKJPS-UHFFFAOYSA-M Thiocyanate anion Chemical compound [S-]C#N ZMZDMBWJUHKJPS-UHFFFAOYSA-M 0.000 description 4
- ZMZDMBWJUHKJPS-UHFFFAOYSA-N hydrogen thiocyanate Natural products SC#N ZMZDMBWJUHKJPS-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- DHCDFWKWKRSZHF-UHFFFAOYSA-N sulfurothioic S-acid Chemical compound OS(O)(=O)=S DHCDFWKWKRSZHF-UHFFFAOYSA-N 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- SOIFLUNRINLCBN-UHFFFAOYSA-N ammonium thiocyanate Chemical compound [NH4+].[S-]C#N SOIFLUNRINLCBN-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 230000007547 defect Effects 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
- 230000009977 dual effect Effects 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
- 230000005484 gravity Effects 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 238000005987 sulfurization reaction Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
- F26B21/001—Drying-air generating units, e.g. movable, independent of drying enclosure
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B9/00—Auxiliary systems, arrangements, or devices
- F28B9/08—Auxiliary systems, arrangements, or devices for collecting and removing condensate
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Biomedical Technology (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Inorganic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a device for utilizing desulfurization waste liquid and an operation method thereof. The invention also provides an operation method of the device for utilizing the desulfurization waste liquid, which comprehensively treats the desulfurization liquid and sulfur foam generated in the coking HPF wet desulfurization process, changes waste into valuable, realizes internal circulation and avoids secondary pollution. The production cost is saved, and the automation control and the energy consumption reduction are realized. The device uses a two-conversion two-absorption process to prepare sulfuric acid, uses a vanadium catalyst, and uses a refractory fiber adhesive, a ceramic fiber board and a refractory fiber reinforced coating to improve the catalytic conversion rate of sulfur dioxide, wherein the conversion rate is more than or equal to 99.75 percent.
Description
Technical Field
The invention belongs to the technical field of comprehensive utilization of desulfurization waste liquid, and particularly relates to a device for utilizing desulfurization waste liquid and an operation method thereof.
Background
The existing coking coal gas is desulfurized by adopting an HPF wet liquid phase catalytic method with ammonia as an alkali source, and a large amount of sulfur foam and desulfurization liquid are generated in the desulfurization process. Most of domestic sulfur foams are used for recovering wet sulfur by a filter pressing method or solid sulfur by a sulfur melting kettle, and the sulfur market is greatly restricted because the recovered sulfur has more impurity content and is very difficult to comprehensively utilize. The desulfurization process generates a large amount of harmful substances, the main components of the desulfurization process are thiocyanate, thiosulfate, sulfate and the like, wherein the thiocyanate has strong toxicity, and if the desulfurization solution is directly discharged without harmless treatment, the desulfurization solution seriously pollutes water and the surrounding environment, thereby causing environmental pollution. Because the components of the desulfurization solution are extremely complex, the resource recovery or harmless treatment is quite difficult, which is a great problem troubling the coking production of companies, and if the desulfurization solution and the waste sulfur are not treated, the normal operation of a desulfurization device is directly influenced, and the realization of the overall environmental protection target of the companies is influenced. The construction of a desulfurization solution treatment facility and the realization of resource utilization by comprehensive utilization of waste sulfur and desulfurization solution become problems which need to be solved by the development of companies, so investment for construction of devices for treating coking desulfurization solution and sulfur foam and producing sulfuric acid by comprehensive utilization of sulfur resources is proposed.
The device comprehensively treats the desulfurization liquid and sulfur foam generated in the coking HPF wet desulfurization process, and ensures the continuous and stable operation of a coke oven gas desulfurization system. By adopting advanced process flow, technical equipment and control means, the dual purposes of pollution control and comprehensive utilization of resources are realized.
The main components of the large amount of salt-containing waste liquid generated in the desulfurization process of the coke oven gas are thiocyanate, thiosulfate, sulfate and the like, wherein the thiocyanate has strong toxicity, and the desulfurization liquid can cause serious pollution to the environment if being directly discharged without harmless treatment.
A large amount of sulfur foam is generated in the wet desulfurization process of coal gas, and the recovered sulfur contains a large amount of impurities at present, so that the sulfur is difficult to comprehensively utilize, can only be treated at extremely low cost, and is not good in sale. Therefore, the advanced process technology is adopted, the desulfurization solution and the sulfur foam are effectively utilized to prepare the sulfuric acid, the sulfuric acid is recycled, and the method has very important significance for the development of national economy and environmental protection.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide a device for utilizing desulfurization waste liquid and an operation method thereof, which comprehensively treat desulfurization liquid and sulfur foam generated in the coking HPF wet desulfurization process, change waste into valuable, realize internal circulation and avoid secondary pollution. The production cost is saved, and the automation control and the energy consumption reduction are realized.
The technical scheme is as follows:
a device for utilizing desulfurization waste liquid comprises a pretreatment adjusting working section, a drying solidification and tail gas working section, a sulfur burning working section, a cooling working section, a washing working section, a conversion absorption working section and a tail gas treatment working section.
All the desulfurization waste liquid in the pretreatment adjusting working section, the drying and curing working section and the tail gas working section is connected with a storage tank to a centrifuge 10 and a filter 13 through a steel skeleton PE pipeline. The exhaust gas generated by the evaporator 8, the evaporator tank 9 and the first and second dryers 1 and 2 is connected to the off-gas tower 6 through stainless steel pipes. The sulphur solid mixture produced by the second dryer 2 is connected to a storage hopper 16 of the sulphur incineration plant by a conveyor 15.
An incinerator 19 of a sulfur incineration working section is connected with a cooling working section boiler 20 through an integrated pouring special high-temperature pipeline, and the cooling working section boiler 20 is connected with a washing working section power wave 21 through a Venturi 4 pipeline. The dynamic wave 21 in the cooling section is connected with a washing tower 22, a degassing tower 23 and an electric demisting tower 24 through glass fiber reinforced plastic pipelines. The cooling section electric demisting 24 is connected with a conversion absorption section drying tower 25 through a stainless steel pipeline, the drying tower 25 is connected with a conversion section through a stainless steel pipeline, and the converted gas in the conversion section is connected with a first absorption tower 26 through a stainless steel pipeline. The first absorption tower 26 is connected to the conversion section through a stainless steel pipe. The conversion section is connected to the second absorption tower 27 through a stainless pipe. All pipelines for conveying sulfuric acid and contacting sulfuric acid in the conversion absorption section adopt a 316L plus anode protection mode.
The tail gas generated in the conversion absorption working section is connected with an activated carbon adsorption tower in the tail gas working section through a glass fiber reinforced plastic pipeline.
The device is mainly divided into two large areas. The first large area is a pretreatment adjusting working section and a drying curing and tail gas working section, the pretreatment adjusting working section and the drying curing working section are both arranged in the same frame factory building, and a left-right distribution mode is adopted to realize function division. Sharing the same underground conditioning tank. The second large area is a sulfur burning section, a cooling section, a washing section, a conversion absorption section and a tail gas treatment section. The area is provided with different functional buildings such as a sulfur burning section frame, a cooling section frame, a conversion absorption frame and a tail gas treatment frame in the same device area. All the working sections are connected through pipelines made of different materials, and function partitioning is achieved.
The operation method of the device for utilizing the desulfurization waste liquid comprises the following steps:
a) and (3) a pretreatment adjusting process, wherein after ammonia water passing through a condensing pump room in a coking plant is filtered by a brown corundum ultrafilter, the content of tar at an outlet is controlled to be 20mg/L, and then the filtered ammonia water enters a desulfurization system of the coking plant, and the step is to intercept a large amount of tar and ensure the quality of products produced in a subsequent drying and curing process. The ammonia water filtered by the brown corundum ultrafilter enters a desulfurization system for desulfurization, the generated desulfurization waste liquid enters an underground adjusting tank 7, is adjusted by a centrifugal machine and a filter 13, and enters a sulfur slurry intermediate tank 11 for stirring after reaching the concentration of 49-53 percent, and then enters a sulfur slurry tank. And a part of the centrifugally filtered clear liquid enters a clear liquid tank 12, is pumped into an evaporator tank 9 through a centrifugal pump and then enters an evaporator 8, other clear liquid returns to the owner desulfurization section, and the evaporated clear liquid is pumped into a sulfur slurry intermediate tank 11 through a pump after the concentration of the evaporated clear liquid meets the requirement and is mixed with the centrifugally filtered sulfur slurry. And pumping the adjusted sulfur slurry in the sulfur slurry tank into a dryer through a screw pump, and performing a drying and curing process. The sulfur solid mixture solidified into particles with the diameter less than 2mm is conveyed by a conveyor after being discharged from the dryer, can be independently packaged for sale or stored, and can also directly enter a subsequent working section through the conveyor 15. And the generated tail gas enters a tail gas treatment process. The tank farm employs an integrated negative pressure process to treat the fugitive gases.
b) The obtained solid sulfur mixture enters an incinerator for incineration through conveying equipment, the incineration temperature is 950-1150 ℃, air supplement is carried out through a furnace bottom fan 18, the gas flow rate is 1.5-2.2 m/s, the residence time of the sulfur solid mixture in the incinerator is 15-22 seconds, and the concentration of sulfur dioxide in the incinerated gas is 10-13%. The specific concentration can be adjusted by frequency conversion of the furnace bottom fan 18. The furnace bottom fan room 40 is a frame structure for placing equipment.
c) And c, cooling, washing, converting and absorbing the high-temperature gas containing the sulfur dioxide in the step b, and treating tail gas to obtain sulfuric acid. The whole process is automatically controlled by a DCS system.
Further, in the step a), the concentration of the filtered clear liquid is about 49-53%, and the suspended sulfur content in the clear liquid after centrifugal filtration is determined according to the storage size of all storage tanks in 12 hours of the total amount: less than or equal to 200 mg/L. Use steam in evaporimeter and the drying-machine in the regulation process and all come from the saturated steam in follow-up boiler, steam gets into condensate recovery unit behind the trap, does the companion heat for all equalizing basins and surge tank, finally merges the circulating water station, compares other projects and uses steam companion heat, and the effective energy saving of this method combines the rationalization inner loop of workshop section around, and all equalizing basins surge tank all set up air pipe connection centrifugal fan 3, set up all jar bodies to-300 Pa negative pressure. The gas is sent to the tail gas treatment process.
Further, the tail gas treatment process comprises the following steps:
1) the air inlet of the dryer is provided with a preheater, the air inlet temperature is ensured to be more than or equal to 75 ℃, the generated tail gas enters the venturi 4 through the stainless steel air pipe, and weak dust is captured through reverse spraying contact. The circulating water in the venturi 4 comes from the condensed water in the subsequent condenser 5. The circulating liquid returns to the ammonium sulfate workshop section of the owner.
2) The tail gas is washed by the Venturi 4 and then enters the condenser 5 for condensation, the condensed evaporation condensate water is used as circulating liquid replenishing liquid in the Venturi 4, the condensed tail gas enters the tail gas tower 6 from the bottom through the centrifugal fan 3, the inlet pressure of the centrifugal fan is-400 Pa, 15% dilute acid is sprayed from the top of the tower in the tail gas tower 6, and the tail gas are fully reacted and absorbed. The dilute acid in the tail gas tower 6 comes from an activated carbon adsorption tower in a sulfuric acid tail gas treatment section. And diluted acid is supplemented and redundant circulating liquid is pumped into an ammonium sulfate working section through a PH monitoring table arranged in the tower.
3) If only the desulfurization waste liquid is sold as a commodity and no dilute sulfuric acid is available in the subsequent working section, the washing liquid in the tail gas working section is changed into ammonium sulfate mother liquid from an owner, the ammonium sulfate mother liquid enters the regulating tank and then is pumped into the tail gas tower 6, and the ammonium sulfate mother liquid is pumped out through the circulating pump of the washing tower to form closed circulation.
4) The treatment method combines the front and the back, thereby avoiding secondary pollution.
Further, in the step c), the outlet temperature of the high-temperature gas containing sulfur dioxide is 1000 +/-150 ℃, the high-temperature gas enters through the inlet of the boiler, the outlet temperature is kept at 320 +/-20 ℃ after the high-temperature gas is cooled, and the boiler generates low-pressure saturated steam. Saturated steam pressure is 2.5 MPa. The generated steam can be used by a dryer at the preorder section through a pressure reducing valve, and the redundant steam can be in parallel with an owner pipe network, so that the self-production and self-sale of energy are realized, and the maximum utilization is realized.
Further, in the step c), the gas washing step includes the following equipment and steps.
1) The gas cooled by the boiler enters dynamic waves, 15-30% dilute sulfuric acid is sprayed into the venturi 4 pipe, and the dilute sulfuric acid is contacted with the gas in the venturi 4 pipe, so that the gas humidity is increased, the gas is cooled, and dust is effectively removed;
2) after being washed by a Venturi 4 tube, the gas is supplied with air by a degassing tower and enters a washing tower to be reversely contacted and washed with dilute sulfuric acid which is sprayed by 15 to 40 percent on the top of the tower, and impurities in the gas are removed. The dust content after gas purification is lower than 0.4mg/m3If the content of the dust is too high, the catalytic effect in the subsequent conversion process is affected, and the conversion efficiency of the sulfur dioxide is poor. The gas is washed and then electrically demisted 24 to remove acid mist, and the acid mist amount at the outlet is less than or equal to 0.005g/Nm3。
Further, in the step c), the conversion absorption section adopts two-rotation and two-absorption, and the adopted equipment comprises a sulfur dioxide fan 33, a drying tower 25, a first absorption tower 26, a second absorption tower 27, a drying circulation tank 29, a first absorption circulation tank 30, a second absorption circulation tank 31, a drying acid cooler, an absorption acid cooler, a finished product acid cooler and an acid circulation pump. The converter 34 is provided with 5 converter beds, and a first heat exchanger 35, a second heat exchanger 36, a third heat exchanger 37, a fourth heat exchanger 38 and a fifth heat exchanger 39 which correspond to each catalyst bed.
Still further, the two-rotation and two-suction process comprises the following steps:
1) the dry absorption process adopts a three-tower three-groove process, an acid circulation absorption system adopts two acid circulations, and a drying tower adopts 94 wt% of H2SO4The recycle, absorber column, used 98 wt% H2SO4And (6) circulating. The circulating acid cooling system consists of two absorption tower acid coolers and one drying tower acid cooler. The acid cooling circulation system is basically set as follows: tanks, pumps, acid coolers, towers, tanks;
2) after the furnace gas from the purification section is supplemented with a proper amount of air, controlling SO in the furnace gas entering the conversion section28.5 Vol%, entering a drying tower from a bottom air inlet, absorbing water in furnace gas by 94 wt% concentrated sulfuric acid sprayed from the top of the tower to make the water content in the air discharged from the tower less than or equal to 0.1g/Nm3The dried acid after absorbing the moisture flows into an acid circulating tank of a drying tower from the bottom of the tower, is mixed with the acid by an acid circulating pump of the first absorption tower to reach the concentration of 94 wt%, and is sent to an acid cooler of the drying tower by an acid circulating pump of the drying tower for cooling, the cooled concentrated acid enters the drying tower for circulating spraying, and the gas is sent to a third heat exchanger from an outlet of the drying tower through a sulfur oxide fan 33;
3) the gas from the third section of the converter enters a first absorption tower after being cooled by a third heat exchanger, and absorbs SO in furnace gas by 98 wt% concentrated sulfuric acid sprayed from the top of the tower3The absorbed acid flows into an absorption circulation tank 30 from the bottom of the tower, is sent to an acid cooler by an absorption circulation pump for cooling, and the cooled concentrated acid enters a first absorption tower for circulating spraying;
4) the gas from the fifth section of the converter enters a second absorption tower after being cooled by a fifth heat exchanger, and SO in the furnace gas is absorbed by 98 wt% concentrated sulfuric acid sprayed from the top of the tower3The absorbed acid flows into a secondary acid absorption circulating tank from the bottom of the tower, is sent to an acid cooler by a secondary acid absorption circulating pump for cooling, and the cooled concentrated acid enters a second absorption tower for circulating spraying;
5) the absorption acid circulating tank is provided with an automatic water feeder for adding process water, and the concentration of absorption acid is adjusted and controlled. When 93 wt% acid is produced, redundant circulating acid in the absorption circulating tank is connected into the drying tower in series and is led out from the drying acid cooler to be used as a product; when 98 wt% acid is produced, the redundant acid in the absorption circulation tank is taken as a product, discharged from an outlet of an absorption acid cooler, metered by an electromagnetic flowmeter, sent to a concentrated sulfuric acid intermediate tank for storage, and finally sent to a concentrated sulfuric acid storage tank of the existing coking device for self use;
6) in order to add mother acid when the device is driven and facilitate the maintenance of equipment and pipelines, an underground tank 32 and an acid pump are arranged;
7) using SO as cold gas after being dried by drying tower and demisted by wire demister on top of tower2After the pressure of the blower is increased, the blower enters the third heat exchanger and the first heat exchanger in sequence for heating, and then enters the first section of the converter for conversion when the temperature reaches 420 ℃. After the reaction, the temperature of furnace gas is raised to about 585 ℃, and the furnace gas enters a first heat exchanger and comes from SO2The cold gas of the blower exchanges heat and cools, the cooled furnace gas enters the second section of catalyst bed layer of the converter for catalytic reaction, then the furnace gas is discharged from the converter, enters the second heat exchanger for cooling and enters the third section of catalyst bed layer of the converter for further reaction;
8) gas from the outlet of the third section of the converter enters the tube pass of a third heat exchanger, the temperature is reduced to about 180 ℃, the gas enters a first absorption tower, and 98 percent concentrated sulfuric acid is used for circularly absorbing SO in the gas3And after acid mist in the gas is removed by a wire mesh demister at the top of the tower, the gas enters a fifth heat exchanger, a fourth heat exchanger and a second heat exchanger in sequence, and the gas enters a fourth section of catalyst bed layer of the converter after being heated for a second conversion reaction. The gas out of the fourth section bed layer enters a fourth heat exchanger to be cooled to 415 ℃, then enters a fifth section catalyst layer of the converter to react, the gas at the outlet of the fifth section passes through a tube pass of the fifth heat exchanger to be subjected to heat exchange cooling with cold furnace gas, the temperature is reduced to about 165 ℃, the gas enters a second absorption tower, and a small amount of SO in the gas is absorbed3And the absorbed concentrated sulfuric acid enters a finished acid tank after passing through a finished acid cooler, and the finished acid is pumped into a finished acid tank area through a finished acid pump. Or transported by automobile according to special conditions;
9) two electric heating furnaces are arranged for heating the furnace gas during the driving. In order to adjust and control the temperature of the conversion section, necessary process pipeline secondary lines and adjusting valves are arranged;
10) and finally, the gas discharged from the second absorption tower enters a patent tail gas treatment device, and is discharged after reaching the standard after treatment.
This device adopts desulfurization waste liquid system acid, and the desulfurization waste liquid comes from coking plant desulfurization system, and the desulfurization waste liquid reaches the saturation after the circulation, and this device is through centrifugation and filtration back, intercepts a large amount of suspended sulfur, filters into the clear solution with the desulfurization waste liquid, returns desulfurization system and continues to use. The device becomes an environment-friendly device which can coexist with a desulfurization system of a coking plant.
The device mainly relates to the following reaction formula:
S+O2＝SO2
NH4SCN+3O2--N2+CO2+SO2+2H2O
(NH4)2S2O3+5/2O2--N2+2SO2+4H2O
(NH4)2SO3+3/2O2--N2+SO2+4H2O
(NH4)2CO3+3/2O2--N2+CO2+4H2O
the invention has the beneficial effects that:
1. the device takes the waste liquid of the coking plant as the raw material, helps the desulfurization system to solve the problem of saturation of the circulating liquid, changes waste into valuable to produce sulfuric acid, and reduces the production cost;
2. the device utilizes a large amount of heat released in the subsequent process to be converted into saturated steam through the waste heat boiler, and the saturated steam can be used by an evaporator and a dryer in the former process, so that the whole device realizes self production and self marketing, and the front and the back are taken into consideration to form a complete internal circulation system;
3. steam condensate water generated by steam-using equipment of the device exchanges heat with the regulating tank through the condensate water recovery device, so that steam tracing can be saved, and redundant steam is merged into a pipe network to improve economic benefit;
4. 98 percent of industrial sulfuric acid produced by the device can meet the national standard requirement;
5. the washing process of the device can effectively guarantee the subsequent conversion efficiency;
6. the device uses a two-conversion two-absorption process to prepare sulfuric acid, uses a vanadium catalyst, and uses a refractory fiber adhesive, a ceramic fiber board and a refractory fiber reinforced coating to improve the catalytic conversion rate of sulfur dioxide, wherein the conversion rate is more than or equal to 99.75 percent.
Drawings
FIG. 1 is an elevation view of the drying, curing and tail gas section of the apparatus;
FIG. 2 is an elevation view of the pretreatment gas section of the apparatus;
FIG. 3 is a plan view of the pretreatment gas section and the drying, curing and tail gas section of the apparatus;
FIG. 4 is a vertical view of the sulfur burning, cooling and purifying section of the apparatus;
FIG. 5 is an elevation view of the conversion absorption and tail gas section of the apparatus;
FIG. 6 is a plan view of the section of the apparatus for sulfur burning, cooling, purification, conversion, absorption and tail gas;
fig. 7 is a general view of the present apparatus.
Detailed Description
The technical solution of the present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
Referring to fig. 1-7, wherein fig. 1 is an elevation view of a drying, curing and tail gas workshop section of the device, which mainly shows the relationship and relative positions of each equipment floor and the main material trend of the workshop section. The regional structure is an overground two-layer frame structure, and an underground adjusting pool is arranged underground. The produced product is output by the second dryer 2 and then conveyed to a sulfur incineration section through a conveyor 15. The section is connected with a sulfur incineration section.
FIG. 2 is a vertical view of a pre-treated gas workshop section of the device, which mainly shows the relation and relative position of each equipment floor and the main material trend of the workshop section. The regional structure is a two-layer frame structure on the ground, a filter 13 is placed in a local steel structure device at the top of a second floor, and a rain shelter is arranged. Other equipment is arranged in the frame structure, and materials are conveyed to a centrifugal machine and a filter 13 through a pump and then automatically flow into a sulfur slurry intermediate tank 11, a clear liquid tank 12 and a sulfur slurry tank 14 through gravity. The prepared slurry in the slurry tank 14 is sent to the first dryer 1 by a pump. The working section is connected with a drying, curing and tail gas working section. A rainproof awning is arranged above the filter 13.
FIG. 3 is a plan view of the pretreatment gas section and the drying, curing and tail gas section of the apparatus, which mainly shows the relative positions of the devices. And overall layout within the region.
Fig. 4 is a vertical view of the sulfur burning, cooling and purifying section of the device, which mainly shows the relationship and relative position of each equipment floor and the main material trend of the section. The waste gas is conveyed by a conveyor 15 in a drying solidification and tail gas working section into a storage hopper 16 in a sulfur incineration working section and then into an incinerator 19 through a feeding belt conveyor 17. The furnace gas after burning in the incinerator 19 is connected with a cooling section boiler 20 through a high-temperature flue gas pipeline, the gas after being cooled by the boiler is connected with a purification section power wave 21, and then is connected with a washing tower 22, a degassing tower 23 and an electric defogging 24. The electric demisting device 24 is connected with a conversion absorption section drying tower 25 through a stainless steel pipeline.
FIG. 5 is a vertical view of a converting absorption and tail gas section of the device, which mainly shows the relationship and relative positions of the floors of each device and the material trend of the section. The gas from the electric demisting 24 of the purification section is connected to a drying tower 25. The drying tower 25 is connected with the conversion working section through a sulfur dioxide fan 33 and a stainless steel pipeline, and the converted gas in the conversion working section is connected with the first absorption tower 26 through the stainless steel pipeline. The first absorption tower 26 is connected to the conversion section through a stainless steel pipe. The conversion section is connected to the second absorption tower 27 through a stainless pipe. All pipelines for conveying sulfuric acid and contacting sulfuric acid in the conversion absorption section adopt a 316L plus anode protection mode.
FIG. 6 is a plan view of the sulfur burning, cooling, purifying, converting, absorbing and tail gas sections of the device, which shows the main relative position relationship of each section.
Fig. 7 is a general view of the apparatus, showing the overall layout and the relative positions of all the sections.
The above description is only a preferred embodiment of the present invention, and the scope of the present invention is not limited thereto, and any simple modifications or equivalent substitutions of the technical solutions that can be obviously obtained by those skilled in the art within the technical scope of the present invention are within the scope of the present invention.
Claims (8)
1. The utility model provides a device that utilizes desulfurization waste liquid which characterized in that: a pretreatment adjusting working section, a drying solidification and tail gas working section, a sulfur burning working section, a cooling working section, a washing working section, a conversion absorption working section and a tail gas treatment working section;
all the desulfurization waste liquid in the pretreatment adjusting working section, the drying and curing working section and the tail gas working section is connected with a storage tank to a centrifugal machine (10) and a filter (13) through a steel skeleton PE pipeline; waste gas generated by the evaporator (8), the evaporator tank (9), the first dryer (1) and the second dryer (2) is connected to a tail gas tower (6) through stainless steel pipelines; the sulfur solid mixture generated by the second dryer (2) is connected with a storage hopper (16) of a sulfur incineration workshop section through a 15-conveyor;
an incinerator (19) of a sulfur incineration working section is connected with a cooling working section boiler (20) through an integrated pouring special high-temperature pipeline, and the cooling working section boiler (20) is connected with a washing working section power wave (21) through a Venturi (4) pipeline; the dynamic wave (21) in the cooling section is connected with a washing tower (22), a degassing tower (23) and an electric demisting tower (24) through glass fiber reinforced plastic pipelines; the cooling section electric demisting device (24) is connected with a conversion absorption section drying tower (25) through a stainless steel pipeline, the drying tower (25) is connected with a conversion section through a sulfur dioxide fan (33) and the stainless steel pipeline, and gas converted in the conversion section is connected with a first absorption tower (26) through the stainless steel pipeline; the first absorption tower (26) is connected with the conversion working section through a stainless steel pipeline; the conversion section is connected with a second absorption tower (27) through a stainless steel pipeline; all pipelines for conveying sulfuric acid and contacting sulfuric acid in the conversion absorption section adopt a 316L plus anode protection mode.
2. An operation method of the apparatus for utilizing a desulfurization waste liquid, characterized in that: the method comprises the following steps:
a) a pretreatment adjusting process, wherein after ammonia water passing through a condensing pump room in a coking plant is filtered by a brown corundum ultrafilter, the content of tar at an outlet is controlled to be 20mg/L, and then the filtered ammonia water enters a desulfurization system of the coking plant, and the step is to intercept a large amount of tar and ensure the quality of products produced in a subsequent drying and curing process; ammonia water filtered by a brown corundum ultrafilter enters a desulfurization system for desulfurization, generated desulfurization waste liquid enters an underground regulating reservoir, is regulated by a centrifugal machine and a filter, sulfur slurry with proper concentration enters a sulfur slurry intermediate tank (11) for stirring, then enters the sulfur slurry tank, part of centrifugally filtered clear liquid enters a clear liquid tank (12), is pumped into an evaporator by a centrifugal pump, other clear liquid returns to an owner desulfurization section, and the evaporated clear liquid with the concentration meeting the requirement is pumped into the sulfur slurry intermediate tank (11) by a pump to be mixed with the centrifugally filtered sulfur slurry; pumping the adjusted sulfur slurry in the sulfur slurry tank into a dryer through a screw pump, and performing a drying and curing process; allowing the mixture to solidify into a sulphur solid mixture having a particle size of less than 2 mm; after being discharged from the dryer, the dried materials are conveyed by a closed conveyor, independently packaged for sale or storage, or directly enter a subsequent working section through a conveyor 15; the generated tail gas enters a tail gas treatment process; the tank area adopts an integral negative pressure process to treat the sporadic gas;
b) the obtained solid sulfur mixture enters an incinerator for incineration through conveying equipment, the incineration temperature is 950-1150 ℃, air supplement is carried out through a blower, the gas flow rate is 1.5-2.2 m/s, the residence time of the sulfur solid mixture in the incinerator is 15-22 s, and the concentration of sulfur dioxide in the incinerated gas is 10-13%; the specific concentration can be adjusted through frequency conversion of the fan;
c) cooling, washing, converting and absorbing the high-temperature gas containing sulfur dioxide in the step b), and treating tail gas to obtain sulfuric acid; the whole process is automatically controlled by a DCS system.
3. The method of operating an apparatus for utilizing a desulfurization waste liquid according to claim 2, characterized in that: in the step a), the concentration of the filtered clear liquid is 40-50% after the filtering by a centrifugal machine and a high-precision filter, all storage tanks are used as the basis of storage size according to 12 hours of the total amount, and the content of suspended sulfur in the clear liquid after the centrifugal filtering is as follows: less than or equal to 200 mg/L; in the adjusting procedure, steam used in an evaporator and a dryer comes from saturated steam in a subsequent boiler, the steam enters a condensate water recovery device after passing through a drain valve, all adjusting tanks and adjusting tanks are subjected to heat tracing and finally merged into a circulating water station, all adjusting tanks of the adjusting tanks are provided with ventilating pipes to be connected with a fan, and all tank bodies are set to be negative pressure of-300 Pa; the gas is sent to the tail gas treatment process.
4. The method of operating an apparatus for utilizing a desulfurization waste liquid according to claim 2, characterized in that: the tail gas treatment process comprises the following steps:
step 1, arranging a preheater at an air inlet of a dryer to ensure that the air inlet temperature is more than or equal to 75 ℃, enabling tail gas to enter a Venturi (4) scrubber through a stainless steel air pipe, and capturing weak dust through reverse spray contact in the Venturi (4) scrubber; the circulating water in the Venturi (4) comes from the condensed water in the subsequent condenser (5); circulating liquid
Step 2, after the tail gas is washed by the Venturi (4), the tail gas enters the condenser (5) for condensation, the condensed evaporated condensate water is used as circulating liquid replenishing liquid in the Venturi (4), the condensed tail gas enters the tail gas washing tower from the bottom through the centrifugal fan, the inlet pressure of the centrifugal fan is-400 Pa, and 15% dilute acid is sprayed from the top of the washing tower to be fully reacted and absorbed with the tail gas; dilute acid in the washing tower comes from a sulfuric acid tail gas treatment section; replenishing dilute acid and pumping redundant circulating liquid into an ammonium sulfate working section through a pH monitoring table arranged in the tower;
and 3, if the desulfurization waste liquid is only sold as a commodity and no dilute sulfuric acid is available in a subsequent workshop section, the washing liquid in the tail gas workshop section is changed into ammonium sulfate mother liquid from a main owner, the ammonium sulfate mother liquid enters the regulating tank and then is pumped into the washing tower, and the ammonium sulfate mother liquid is pumped out through a circulating pump of the washing tower to form closed circulation.
5. The method of operating an apparatus for utilizing a desulfurization waste liquid according to claim 2, characterized in that: in the step c), the outlet temperature of the high-temperature gas containing sulfur dioxide is 1000 +/-150 ℃, the high-temperature gas enters through the inlet of the waste heat boiler, the outlet temperature is kept at 320 +/-20 ℃ after cooling, and the boiler generates low-pressure saturated steam; saturated steam pressure is 2.5 MPa.
6. The method of operating an apparatus for utilizing a desulfurization waste liquid according to claim 2, characterized in that: in the step c), the gas washing process comprises the following equipment and processes;
step 1, feeding gas cooled by a boiler into a dynamic wave, spraying 15-30% dilute sulfuric acid into a Venturi (4) tube, and contacting the dilute sulfuric acid with the gas in the Venturi (4) tube to increase the humidity of the gas, cool and cool the gas and effectively remove dust;
step 2, after the gas is washed by dynamic waves, the gas is supplied by a degassing tower, enters a filler washing tower, and is reversely contacted and washed with 15-40% diluted sulfuric acid sprayed on the top of the tower to remove impurities in the gas; the dust content after gas purification is lower than 0.4mg/m3If the content of the dust is too high, the catalytic effect in the subsequent conversion process is influenced, so that the conversion efficiency of the sulfur dioxide is poor; washing the gas, electrically demisting to remove acid mist, wherein the amount of the acid mist at the outlet is less than or equal to 0.005g/Nm3。
7. The method of operating an apparatus for utilizing a desulfurization waste liquid according to claim 2, characterized in that: in the step c), the conversion and absorption section adopts two-rotation and two-absorption, and the adopted equipment comprises a sulfur dioxide fan, a drying tower, a first absorption tower, a second absorption tower, a drying acid tank, an absorption acid tank, a drying acid cooler, an absorption acid cooler, a finished product acid cooler and an acid circulating pump; the system is provided with a converter with 5 converter beds and a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger and a fifth heat exchanger which correspond to each catalyst bed.
8. The method of operating an apparatus for utilizing a desulfurization waste liquid according to claim 7, characterized in that: the two-rotation and two-suction process comprises the following steps:
step 1, the dry absorption process adopts a three-tower three-groove process, an acid circulation absorption system adopts two acid circulations, and a drying tower adopts 94 wt% of H2SO4The recycle, absorber column, used 98 wt% H2SO4Circulating; two absorption towers, an acid cooler anda drying tower acid cooler forms a circulating acid cooling system; the acid cooling circulation system is basically set as follows: tanks, pumps, acid coolers, towers, tanks;
step 2, after the furnace gas from the purification section is supplemented with a proper amount of air, controlling SO in the furnace gas entering the conversion section28.5 Vol%, entering a drying tower from a bottom air inlet, absorbing water in furnace gas by 94 wt% concentrated sulfuric acid sprayed from the top of the tower to make the water content in the air discharged from the tower less than or equal to 0.1g/Nm3The dried acid after absorbing the moisture flows into a drying circulating tank (29) from the bottom of the tower, is mixed to 94 wt% concentration by an acid circulating pump of a first absorption tower, is sent to a drying tower acid cooler by a drying tower acid circulating pump for cooling, and the cooled concentrated acid enters a drying tower for circulating spraying;
step 3, cooling the gas from the third section of the converter by a third heat exchanger, then introducing the gas into a first absorption tower, and absorbing SO in furnace gas by 98 wt% concentrated sulfuric acid sprayed from the top of the tower3The absorbed acid flows into an absorption circulation tank (30) from the bottom of the tower, and is sent to an acid cooler for cooling by an absorption circulation pump, and the cooled concentrated acid enters a first absorption tower for circular spraying;
step 4, cooling the gas from the fifth section of the converter by a heat exchanger V, then entering a second absorption tower, and absorbing SO in furnace gas by 98 wt% concentrated sulfuric acid sprayed from the top of the tower3The absorbed acid flows into a secondary absorption circulating tank (31) from the bottom of the tower, is sent to an acid cooler by a secondary absorption circulating pump for cooling, and the cooled concentrated acid enters a second absorption tower for circulating spraying;
step 5, arranging an automatic water feeder in the absorption acid circulating tank, adding process water, and adjusting and controlling the concentration of the absorption acid; when 93 wt% acid is produced, redundant circulating acid in the absorption circulating tank is connected into the drying tower in series and is led out from the drying acid cooler to be used as a product; when 98 wt% acid is produced, the redundant acid in the absorption circulation tank is taken as a product, discharged from an outlet of an absorption acid cooler, metered by an electromagnetic flowmeter, sent to a concentrated sulfuric acid intermediate tank for storage, and finally sent to a concentrated sulfuric acid storage tank of the existing coking device for self use;
step 6, arranging an underground acid tank and an acid pump in order to add mother acid when the device is driven and facilitate the maintenance of equipment and pipelines;
step 7, drying the cold gas by a drying tower and demisting the cold gas by a wire mesh demister at the top of the tower by SO2After the pressure of the blower is increased, the blower sequentially enters a heat exchanger III and a heat exchanger I to be heated, and then enters a first section of the converter to be converted when the temperature reaches 420 ℃; after reaction, the temperature of furnace gas rises to 585 ℃, enters a first heat exchanger and comes from SO2The cold gas of the blower exchanges heat and cools, the cooled furnace gas enters the second section of catalyst bed layer of the converter for catalytic reaction, then the furnace gas is discharged from the converter, enters the second heat exchanger for cooling, and enters the third section of catalyst bed layer of the converter for further reaction;
step 8, the gas from the outlet of the third section of the converter enters the tube side of a third heat exchanger, the temperature is reduced to 180 ℃, the gas enters a first absorption tower, and 98 percent concentrated sulfuric acid is used for circularly absorbing SO in the gas3After acid mist in the gas is removed by a wire mesh demister at the top of the tower, the gas enters a fifth heat exchanger, a fourth heat exchanger and a second heat exchanger in sequence, and the gas enters a fourth section of catalyst bed layer of the converter after being heated for a second conversion reaction; the gas out of the fourth section bed layer enters a fourth heat exchanger to be cooled to 415 ℃, then enters a fifth section catalyst layer of the converter to react, the gas at the outlet of the fifth section passes through a tube pass of the fifth heat exchanger to be subjected to heat exchange cooling with cold furnace gas, the temperature is reduced to 165 ℃, the gas enters a second absorption tower, and a small amount of SO in the gas is absorbed3The absorbed concentrated sulfuric acid enters a finished acid tank after passing through a finished acid cooler, and the finished acid is pumped into a finished acid tank area through a finished acid pump; or transported by automobile according to special conditions;
step 9, two electric heating furnaces are arranged for heating the furnace gas during the start-up; in order to adjust and control the temperature of the conversion section, necessary process pipeline secondary lines and adjusting valves are arranged;
and step 10, finally, the gas discharged from the second absorption tower enters a patent tail gas treatment device, and is discharged after reaching the standard after treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010195400.8A CN111232934A (en) | 2020-03-19 | 2020-03-19 | Device for utilizing desulfurization waste liquid and operation method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010195400.8A CN111232934A (en) | 2020-03-19 | 2020-03-19 | Device for utilizing desulfurization waste liquid and operation method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111232934A true CN111232934A (en) | 2020-06-05 |
Family
ID=70875389
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010195400.8A Pending CN111232934A (en) | 2020-03-19 | 2020-03-19 | Device for utilizing desulfurization waste liquid and operation method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111232934A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112408422A (en) * | 2020-09-29 | 2021-02-26 | 宁波中科远东催化工程技术有限公司 | Production of H from sulfur-containing waste2SO4System and method |
| CN113968574A (en) * | 2021-11-26 | 2022-01-25 | 山东绿知源环保工程有限公司 | Process for efficiently separating elemental sulfur from desulfurization solution and sulfur foam |
| CN116101982A (en) * | 2023-01-09 | 2023-05-12 | 江苏吉华化工有限公司 | Sulfur acid making system and method |
| CN116812878A (en) * | 2023-04-01 | 2023-09-29 | 江苏田润化工设备有限公司 | A desorption purifier for refining sulfuric acid production |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104326486A (en) * | 2014-10-30 | 2015-02-04 | 济南冶金化工设备有限公司 | Device for producing ammonium sulfate by using waste sulphur generated during gas desulfuration |
| CN107954403A (en) * | 2018-01-08 | 2018-04-24 | 上海乐谦工程科技有限公司 | A kind of resource-conserving spent acid treatment process and device |
| CN109534301A (en) * | 2019-01-03 | 2019-03-29 | 众德环保科技有限公司 | A kind of oxygen-enriched acid-making process of sulfur-containing smoke gas double-absorption |
| CN110217760A (en) * | 2019-05-23 | 2019-09-10 | 北京科技大学 | A kind of desulphurization waste liquid of coke oven gas relieving haperacidity preparation process |
| CN110734209A (en) * | 2019-10-22 | 2020-01-31 | 浙江环兴机械有限公司 | Operation method of industrial solid waste and sludge rotary kiln co-processing integrated device |
| CN212687568U (en) * | 2020-03-19 | 2021-03-12 | 四川华茂聚源建筑工程设计有限公司 | Device for utilizing desulfurization waste liquid |
-
2020
- 2020-03-19 CN CN202010195400.8A patent/CN111232934A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104326486A (en) * | 2014-10-30 | 2015-02-04 | 济南冶金化工设备有限公司 | Device for producing ammonium sulfate by using waste sulphur generated during gas desulfuration |
| CN107954403A (en) * | 2018-01-08 | 2018-04-24 | 上海乐谦工程科技有限公司 | A kind of resource-conserving spent acid treatment process and device |
| CN109534301A (en) * | 2019-01-03 | 2019-03-29 | 众德环保科技有限公司 | A kind of oxygen-enriched acid-making process of sulfur-containing smoke gas double-absorption |
| CN110217760A (en) * | 2019-05-23 | 2019-09-10 | 北京科技大学 | A kind of desulphurization waste liquid of coke oven gas relieving haperacidity preparation process |
| CN110734209A (en) * | 2019-10-22 | 2020-01-31 | 浙江环兴机械有限公司 | Operation method of industrial solid waste and sludge rotary kiln co-processing integrated device |
| CN212687568U (en) * | 2020-03-19 | 2021-03-12 | 四川华茂聚源建筑工程设计有限公司 | Device for utilizing desulfurization waste liquid |
Non-Patent Citations (1)
| Title |
|---|
| 白玮: "焦化低品质硫磺及脱硫废液焚烧制酸工艺", 燃料与化工, vol. 46, no. 6, pages 56 - 60 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112408422A (en) * | 2020-09-29 | 2021-02-26 | 宁波中科远东催化工程技术有限公司 | Production of H from sulfur-containing waste2SO4System and method |
| CN113968574A (en) * | 2021-11-26 | 2022-01-25 | 山东绿知源环保工程有限公司 | Process for efficiently separating elemental sulfur from desulfurization solution and sulfur foam |
| CN116101982A (en) * | 2023-01-09 | 2023-05-12 | 江苏吉华化工有限公司 | Sulfur acid making system and method |
| CN116101982B (en) * | 2023-01-09 | 2024-06-14 | 江苏吉华化工有限公司 | Sulfur acid making system and method |
| CN116812878A (en) * | 2023-04-01 | 2023-09-29 | 江苏田润化工设备有限公司 | A desorption purifier for refining sulfuric acid production |
| CN116812878B (en) * | 2023-04-01 | 2024-06-07 | 江苏田润化工设备有限公司 | A desorption purifier for refining sulfuric acid production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111232934A (en) | Device for utilizing desulfurization waste liquid and operation method thereof | |
| US20160030883A1 (en) | Method and apparatus for treating acidic tail gas by using ammonia process flue gas | |
| CN110217760B (en) | Preparation process for preparing acid from coke oven gas desulfurization waste liquid | |
| CN110272082B (en) | Desulfurization waste water evaporation crystallization coupling flue gas reheat integrated system | |
| CN101723334A (en) | Raw material pretreatment process for preparing sulfuric acid by using low-quality sulfur and sulphur-bearing waste solution | |
| CN108554157A (en) | A kind of single column washing Wet fume sweetening dust remover of no stock tank secondary cycle | |
| CN205653162U (en) | System for sulphuric acid is prepared to sulphur waste liquid that contains that utilizes coal gas wet oxidation process to produce | |
| CN201658945U (en) | Sintering flue gas purification system based on heat pipe waste heat recovery technology | |
| CN113357652A (en) | Treatment method of desulfurization waste liquid and sulfur foam | |
| CN112206641A (en) | Single-tower multistage circulating ammonia/ammonium sulfate method for flue gas desulfurization | |
| CN102887529B (en) | Ammonium sulfate production system and preparation method thereof | |
| CN212687568U (en) | Device for utilizing desulfurization waste liquid | |
| CN203886407U (en) | Flue gas purification and deep afterheat recycling integrated device | |
| CN208742284U (en) | A kind of single column washing Wet fume sweetening dust remover of no stock tank secondary cycle | |
| CN102512910B (en) | Smoke heat exchange process for recycling evaporated water of gas desulfurization system | |
| CN101774550B (en) | Novel production method of sulfuric acid | |
| CN205156423U (en) | Exhaust purification and waste heat recovery use multipurposely system | |
| CN217961993U (en) | Ammonia process desulfurization and decarbonization tower and chemicals coproduction device | |
| CN101757843B (en) | Improved process for performing ammonium sulfite pulping by using sulfur-containing flue gas absorber | |
| CN203558850U (en) | Sulfur-containing waste liquid dry method acid making system | |
| CN206082090U (en) | Absorption formula flue gas waste heat utilization , purification, dehydrating unit with multichannel circulation | |
| CN112717652B (en) | Integrated energy-saving environment-friendly ammonia desulphurization crystallization system and method | |
| CN214437776U (en) | Integrated energy-saving environment-friendly ammonia desulfurization crystallization system | |
| CN211753907U (en) | Efficient direct contact type condensation system for eliminating white smoke plume by wet desulphurization | |
| CN214437829U (en) | Energy-saving environment-friendly ammonia desulphurization zero-emission system of sulfur recovery device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20200605 |