CN206051573U - A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant - Google Patents
A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant Download PDFInfo
- Publication number
- CN206051573U CN206051573U CN201621014297.8U CN201621014297U CN206051573U CN 206051573 U CN206051573 U CN 206051573U CN 201621014297 U CN201621014297 U CN 201621014297U CN 206051573 U CN206051573 U CN 206051573U
- Authority
- CN
- China
- Prior art keywords
- washing
- absorption tower
- tail gas
- fluorine
- wet
- 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.)
- Expired - Fee Related
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant, using 80m high altitude discharges after " a fluorine washing absorption tower → Venturi scrubbing absorber → difluoro washing absorption tower → trifluoro washing absorption tower → washing tail gas absorption tower " Pyatyi countercurrent washing absorption pattern washing absorption, as a fluorine scrubbing tower washing absorption liquid (predominantly H2SiF6) washing tail gas absorption system is discharged after solution concentration >=10% go hexafluosilicic acid storage tank to settle, as Na after the recovered dissolving iodine therein of supernatant2SiF6Workshop and anhydrous HF workshop raw material, bottom settle silica gel as white carbon workshop raw material.This utility model has Wet-process Phosphoric Acid Production washing tail gas assimilation effect substantially, and in tail gas, fluorine silicon iodine resource recycling rate is high, and plant automation degree is high and the low advantage of operation expense.
Description
Technical field
This utility model is related to Wet-process Phosphoric Acid Production washing tail gas absorption plant, belongs to phosphorous chemical industry production field.
Background technology
Fluorine silicon materials are widely used in military project, Aero-Space, petrochemical industry, e-mail as important new chemical materialses
The field such as breath, automobile, light textile, medicine, agricultural, environmental protection, food and new forms of energy and emerging strategic industries.Through more than 50 years send out
Exhibition, China's fluorine silicon materials industry have formed covering extensive fields, and industrial chain is complete, and produce with the new and high technology of other industries highlights correlations
Industry, meanwhile, China has become global fluorine silicon materials production and consumption big country.
In nature, fluorine resource is mainly derived from natural cryolite, fluorite and rock phosphate in powder.Wherein, natural cryolite number
Amount is few, and commercial development value is low.In the fluorination product salt of China 30wt/a, about 88% fluorine comes from fluorite.With fluorination
Chemical product demand grows with each passing day, and the consumption of fluorite is incrementally increased, and existing fluorite reserves are only capable of meeting China's fluorination work about 20
The development in year, is the sustainable development for realizing fluorine chemical industry, need to develop other fluorine resource comprehensive utilization technologies.Contain in rock phosphate in powder
There is a certain amount of fluorine, a large amount of fluoro-gas and silica gel precipitation can be produced during Wet-process Phosphoric Acid Production, in non-renewable money
Source today in short supply, in research Wet-process Phosphoric Acid Production tail gas, fluorine silicon resource recovery technology is particularly important.
The vertical utilization of reported phosphorus ore association fluorine silicon resource comprehensive utilization technique You Nanhua group companies Shack contains at present
Fluorine waste gas produces fluoride and white carbon, prepares sodium fluoride and white carbon by hexafluosilicic acid and soda reaction；Shanghai dimension comes modern section
Skill Development Co., Ltd has applied for prodan the patent of invention that white carbon is prepared as raw material；Yunnan Yuntianhua world chemical industry stock
Part company limited works out the process route that the ammonification of phosphoric acid by wet process by-product fluosilicic acid produces high-reinforcement white carbon black.Product silica gel in phosphate fertilizer industry
Can be used to prepare waterglass, white carbon, 4A type molecular sieves, metasilicate pentahydrate sodium, carborundum and monocrystal silicon etc..In view of traditional work
In skill, Wet-process Phosphoric Acid Production washing tail gas absorbing liquid-hexafluosilicic acid concentration is relatively low and impurity content is high, the efficient synthesis of fluorine silicon resource
Using being restricted.Currently, sulphur dioxide of phosphor chemical industry mainly using the hexafluosilicic acid and silica gel obtained during wet-process phosphoric acid concentration for original
Material carries out the further deep processing of fluorine silicon resource.
Phosphate Rock of China usage amount is about 30000kt/a, and wherein mainly in the form of fluor-apatite, fluorine is accounted for association fluorine
The mass fraction of rock phosphate in powder is about 3%-4%.During concentrated sulphuric acid decomposing rock phosphate with hydrogen, the gas phase escaped quantity of fluorine is about 5%-
10%, it is about 25%-30% in ardealite, is about 65%-70% in phosphoric acid, enters during Phosphoric Acid Concentration
The fluorine of gas phase is about 38%-45%.Currently, Kweiyang is opened phosphatization fertilizer company limited phosphoric acid workshop phosphoric acid extraction workshop section and possesses 72wt
(P2O5)/a phosphoric acid by wet process production capacities, due to SiO in rock phosphate in powder2It is excessive, therefore fluoride is mainly with H in liquid phase2SiF6Form is present, tail
The 100%H that gas washing absorption system is produced2SiF6Amount is about 1.4wt/a, 100%SiO2Amount is about 2900t/a.From environmental protection and fluorine
From the point of view of silicon resource comprehensive utilization, it is necessary to which Wet-process Phosphoric Acid Production tail gas is processed.From suitable washing absorption side
It is significant for phosphorous chemical industry is produced that method processes Wet-process Phosphoric Acid Production tail gas.
The washing absorption process of Wet-process Phosphoric Acid Production tail gas is a mass-transfer progress, affects its washing absorption efficiency
Factor mainly has the following aspects：
(1) from the exhaust temperature higher (65～75 DEG C) of phosphoric acid by wet process extractive reaction digestive shelf effusion, the evaporation of moisture makes
Tail gas is close to saturation so that the absorption process based on gas-liquid mass transfer cannot almost be carried out, and becomes and saturation water is steamed
The condensation process of gas, needs substantial amounts of washing absorption agent that gas can just condensed out.A large amount of fluorides otherwise in tail gas will
Washing tail gas absorption system is taken out of by uncooled vapor.
(2) SiF in phosphoric acid by wet process extraction tail gas4Content is high, SiF4With the moisture in washing absorption agent in gas liquid film
Place forms SiO2·nH2The colloidal foam layer of O, it will reduce SiF4With the response speed of moisture in washing absorption agent, interface is limited
Chemical reaction process is carried out continuously.Meanwhile, and SiO is separated out in the liquid phase2·nH2O colloids, are easily deposited on absorption inner wall of tower, inhale
Receive on cycles of washing liquid inner-walls of duct and shower nozzle, cause the blocking of washing absorption tower and inner-walls of duct, affect normal production.
(3) in the raw material phosphorus ore that Wet-process Phosphoric Acid Production is used, carbonate and organic components are generally higher, in phosphoric acid by wet process
In extraction process, a large amount of foams can be produced, a large amount of ardealites and mineral powder granular will be carried in foam secretly, and enter fluorine absorption system,
These particulate matters easily with H2SiF6Solution reaction generates the dirty of slightly solubility, causes the stifled of washing absorption tower and inner-walls of duct
Plug, affects normal production.
(4) technological parameter of washing tail gas absorption equipment selects to be also the key factor for affecting washing tail gas absorption efficiency.
At present, reported Wet-process Phosphoric Acid Production washing tail gas absorption technique has WATER-WASHING METHOD, Calx WATER-WASHING METHOD, quick lime
Powder and activated carbon dry process fluorinated tail gas method and ammonia wash method.Wherein WATER-WASHING METHOD process is simple, technology maturation and application is more wide
It is general, currently, adopting "+one fluorine washing absorption tower of venturi+difluoro washing absorption tower " three stage countercurrents more in large-scale the phosphoric acid by wet process workshop
Washing mode, the method mainly generate thing H2SiF6Concentration is relatively low, is directly produced Na2SiF6Or anhydrous HF technical difficulty it is larger and
Production cost is higher.If returning wet phosphoric acid extracting bath easily causes extraction tank and defecator fouling, direct externally discharged waste water station
Not only increase sewage disposal difficulty, while causing the waste of fluorine silicon resource.The H that cannot be arranged outward2SiF6Solution continuously circulates washing and inhales
Receive fluorinated tail gas and easily the foulings such as fluosilicate, silica gel are produced in fluorine absorption system, cause system equipment to block, seriously restrict wet
The raising of method phosphoric acid production device Homes Using TV and produce load.Meanwhile, with H2SiF6Solution concentration is gradually stepped up, and gas-liquid is passed
Matter speed is reduced, and causes washing tail gas assimilation effect poor, makes exhaust emissions index (granular material discharged concentration, granular material discharged
Speed, fluoride emission concentration and fluoride emission speed) cannot generally meet《Discharge standard of air pollutants》
(GB16297-1996) secondary standard limit value is required.Calx WATER-WASHING METHOD makees absorbent washing absorption wet method phosphorus using caustic lime water
Acid production tail gas, its absorption efficiency increase compared with WATER-WASHING METHOD, but fluorine silicon resource recycles difficulty, the party in increased tail gas
Method is mainly for the purpose of purifying emptying tail gas.Calcium lime powder and activated carbon dry process fluorinated tail gas method are will be fluorinated tail gas Jing little
A small amount of H is reclaimed after absorbing in type water mist sprinkling absorption tower2SiF6, while making fluorinated tail gas be humidified, go out tower tail gas and enter in blender,
Sack cleaner dedusting, exhaust emissions after dedusting are entered after fully mixing with the calcium lime powder and activated carbon for spraying into, and removes
It is fluorine-containing ash in landfill yard security landfill.But the method handling process is complex and causes the waste of fluorine resource.Ammonia just washes method
It is absorbing fluoro-gas, to generate (NH by the use of ammonia as absorbent4)2SiF6Solution.The method causes system without H2SiF6
Produce, limit the utilization ways of fluorine silicon resource in tail gas to a certain extent.
Currently, Wet-process Phosphoric Acid Production washing tail gas absorption plant generally adopts impact type scrubber, spray absorption tower, Wen Qiu
In scrubber, horizontal crossing current (cross-flow) sprayer-washer etc..Impact type scrubber spray absorption tower efficiency is low, and emptying end gas are fluorine-containing
Concentration is high, is rarely employed at present.Spray absorption tower efficiency is also low, and emptying end gas fluoro-containing concentration is high, as Yunnan factory was adopted if originally
This scrubber, afterwards reconstruction add two sections of tubulent contact towers for three sections of purification processes, i.e. spray absorption tower, and with 2%Ca (OH)2's
Solution can be reduced as absorbent, emptying end gas fluorinated volume.Venturi scrubber is conventional fluoro-gas cleaning equipment, is lacked
Point is that fluid resistance is big, is easily blocked trunnion by materials such as tail gas association silica gel.Using one-level Venturi scrubber, many factory rows
Empty tail gas still has exceeded phenomenon.Horizontal crossing current (cross-flow) sprayer-washer should be theoretically that good gas purification sets
Standby, its detersive efficiency is very high, more than 99% but unsatisfactory in actual applications, and tail gas association silica gel is easily blocked
Filling system.
The content of the invention
The purpose of this utility model is：A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant is provided, problems with is solved：
(1) Wet-process Phosphoric Acid Production exhaust emissions index (granular material discharged concentration, granular material discharged speed, fluoride are ensured
Concentration of emission and fluoride emission speed) meet《Discharge standard of air pollutants》(GB16297-1996) secondary standard limit
Value is required.
(2) 72wt (P are ensured2O5The 100% of the supporting washing tail gas absorption system generation of)/a wet-process phosphoric acid production plants
H2SiF6Amount >=1.4wt/a, 100%SiO2Amount about >=2900t/a, washing tail gas absorbing liquid-H2SiF6Solution concentration >=10%.
(3) ensure that Wet-process Phosphoric Acid Production washing tail gas absorption systems shuts down cleaning cycle >=60d and shut down clearance time≤
1d。
(4) ensure that Wet-process Phosphoric Acid Production washing tail gas absorption system possesses coproduction Na2SiF6With anhydrous HF function.
(5) ensure that Wet-process Phosphoric Acid Production washing tail gas absorption system possesses iodine and silicon resource recovery function in coproduction tail gas.
To achieve these goals, this utility model employs following technical scheme：
A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant, washes including the fluorine being linked in sequence according to exhaust gas flow direction successively
Absorption tower, Venturi scrubbing absorber, difluoro washing absorption tower, trifluoro washing absorption tower and washing tail gas absorption tower are washed, it is described
One fluorine washing absorption tower is also connected with hexafluosilicic acid storage tank, is also set up between the trifluoro washing absorption tower and washing tail gas absorption tower
There are demister and blower fan, the washing tail gas absorption tower is connected with gypsum stack water return pipeline or 10% ammonia pipeline.
The one fluorine washing absorption tower is provided with two-layer countercurrent spray wash mill.
The difluoro washing absorption tower is provided with two-layer countercurrent spray wash mill.
The trifluoro washing absorption tower is provided with three layers of countercurrent spray wash mill.
The washing tail gas absorption tower is provided with three layers of countercurrent spray wash mill.
Between the washing tail gas absorption tower, trifluoro washing absorption tower, difluoro washing absorption tower and a fluorine washing absorption tower
Connected by flow tube.
Above-mentioned washing tail gas absorption plant can be according to following process operations：
1st, according to Wet-process Phosphoric Acid Production operating mode and exhaust emissions index situation, selectively opened gypsum stack backwater or
10% ammonia valve Jing effusion meters measure 20m3/ h carries out washing tail gas absorption tower and supplements washing absorption liquid, and Jing washing tail gas absorb
Tower spray washing circulating pump carries out three layers of spray washing and absorbs to tail gas, tail gas qualified discharge after washing absorption.
2nd, when it is gypsum stack backwater that the washing of washing tail gas absorption tower supplements washing absorption liquid, when absorbing liquid H2SiF6
Concentration >=1.5%, behind proportion >=1.0, using overflow manner by 10m3/ h absorbing liquids are supplemented to trifluoro washing absorption tower, Jing trifluoros
Washing absorption tower spray washing circulating pump carries out three layers of spray washing and absorbs to tail gas.When washing tail gas absorption tower, washing supplement is washed
Wash absorbing liquid for 10% ammonia when, as absorbing liquid (NH4)2SiF6After concentration >=10%, absorbing liquid is delivered to into anhydrous HF workshop, inhaled
Receive liquid and NH3Further reaction generates NH4F and SiO2·nH2O, NH4F further with dense H2SO4Reaction generates HF and NH4HSO4,
Further the operation such as Jing rectification obtains anhydrous HF product to HF.SiO2·nH2O generates Na with the NaOH solution reaction of heat2SiO3It is molten
Liquid, after being separated by filtration solid phase impurity, adds dense H in filtrate2SO4White carbon precipitation is obtained, white carbon is further across filter and is dried
White carbon black product is obtained etc. operation.At the same time, open gypsum stack backwater valve Jing effusion meters metering 20m3/ h carries out trifluoro
Washing absorption tower supplements washing absorption liquid, and Jing trifluoros washing absorption tower spray washing circulating pump carries out three layers of spray washing to tail gas
Absorb.
3rd, as trifluoro washing absorption tower washing absorption liquid H2SiF6Concentration is 1.0%-1.5%, after proportion is 1.0-1.05,
Difluoro washing absorption tower is supplemented to, Jing difluoros washing absorption tower spray washing circulating pump carries out two-layer spray washing suction to tail gas
Receive.Meanwhile, starting venturi spray washing circulating pump carries out spray washing absorption to tail gas.
4th, as difluoro washing absorption tower washing absorption liquid H2SiF6Concentration is 3.0%-8.0%, after proportion is 1.05-1.08,
A fluorine washing absorption tower is supplemented to, mono- fluorine washing absorption tower spray washing circulating pumps of Jing carry out two-layer spray washing suction to tail gas
Receive.
5th, as a fluorine washing absorption tower washing absorption liquid H2SiF6Concentration >=10.0%, behind proportion >=1.08, opens a fluorine and washes
Wash absorption tower and tube valve is connected to hexafluosilicic acid medial launder, after hexafluosilicic acid medial launder liquid level reaches 45% height, start hexafluosilicic acid
Hexafluosilicic acid is pumped into hexafluosilicic acid storage tank by line pump.After in hexafluosilicic acid storage tank, hexafluosilicic acid once settles 10h, starting hexafluosilicic acid pump will
Hexafluosilicic acid finished product is pumped in the depositing reservoir of villiaumite workshop and carries out secondary settlement.H after clarification is qualified2SiF6Solution delivers to iodine recovery vehicle
Between, H2SiF6The operations such as solution is oxidized successively, extraction, absorption, purification, oxidation are obtained essence iodine product.
6th, open hexafluosilicic acid storage tank and tube valve is connected to silica gel collecting tank, beat after hexafluosilicic acid transfer sky in hexafluosilicic acid storage tank
Hexafluosilicic acid storage tank slag field backwater flushing water valve is opened, starts silica gel groove stirring paddle, when silica gel collecting tank liquid level reaches 50% height
Afterwards, start silica gel pump and silica gel is delivered to into white carbon workshop.
7th, after hexafluosilicic acid tank field geosyncline liquid level reaches 50% height, start geosyncline vertical pump and sewage pumped into into sump,
Washing tail gas absorption tower slag field backwater consumption is now reduced after Sewage slot liquid level reaches 75% height and (after start debugging, determines tool
Volume data).Start sewage vertical pump using sewage as small pump trifluoro washing absorption tower.According to gas-liquid separator fouling condition,
Gas-liquid separator cleaning spray tube valve is opened periodically.
Fresh water (FW) and ammonia absorption fluorinated tail gas ultimate principle are as follows：Wet-process Phosphoric Acid Production tail gas main component is SiF4,
Next to that HF, phosphoric acid steam and drop etc..
Phosphoric acid by wet process extraction production reaction equation：
Ca5(PO4)3F+5H2SO4+10H2O=3H3PO4+5CaSO4·2H2In HF and rock phosphate in powder that O+HF ↑ reaction is generated
SiO2Reaction generates H2SiF6：
6HF+SiO2=H2SiF6+2H2O
H2SiF6Easily further decompose and generate SiF4And HF：
A small amount of H2SiF6With SiO2Reaction generates SiF4：
2H2SiF6+SiO2=3SiF4↑+2H2O
Fluorine in gas phase is mainly with SiF4Form is present, and generates H after washing absorption with water2SiF6Precipitate with silica gel：
3SiF4+(n+2)H2O=2H2SiF6+SiO2·nH2O↓
If (NH is generated after being absorbed with ammonia scrubbing4)2SiF6Precipitate with silica gel：
3SiF4+(n+2)H2O=2H2SiF6+SiO2·nH2O↓
H2SiF6+2NH3=(NH4)2SiF6
(NH4)2SiF6It is soluble in water, with excessive NH3Can decompose during effect reaction：
The reaction is reversible reaction, selects corresponding condition, just can be allowed to toward either direction carry through to the end.
Above-mentioned Wet-process Phosphoric Acid Production washing tail gas absorption plant is by mono- fluorine washing absorption tower countercurrent washings of fluorine silicon tail gas Jing
Venturi scrubbing absorber is entered after absorption, in fluorinated tail gas scripture mound, after the washing of washing absorption device, difluoro washing absorption is entered
Tower, Jing after countercurrent washing absorbs, fluorinated tail gas enter trifluoro washing absorption tower, and Jing after countercurrent washing absorbs, fluorinated tail gas Jing is removed
80m high altitude discharges after washing tail gas absorption tower countercurrent washing absorption are entered by exhaust fan after foam device foam removal；When a fluorine scrubbing tower
After solution concentration >=10% of washing absorption liquid, discharge it washing tail gas absorption system and go to the sedimentation of hexafluosilicic acid storage tank, supernatant
As Na after the recovered dissolving iodine therein of liquid2SiF6Workshop and anhydrous HF workshop raw material, bottom settle silica gel as Linesless charcoal illegal vehicle
Between raw material.
Countercurrent washing liquid in washing tail gas absorption tower is gypsum stack backwater or 10% ammonia.
Washing absorption liquid carries out pressure circulated in countercurrent in each washing absorption equipment.
Wet-process Phosphoric Acid Production washing tail gas absorption plant of the present utility model adopts " fluorine a washing absorption tower → venturi
Washing absorption device → difluoro washing absorption tower → trifluoro washing absorption tower → washing tail gas absorption tower " Pyatyi countercurrent washing absorption side
Formula, will be from mono- fluorine washing absorption tower circulating cleaning solution two-layers of the fluorine silicon tail gas such as phosphoric acid by wet process extractive reaction digestive shelf Jing adverse current
Efficient Venturi scrubbing absorber is entered after washing absorption, is traveled further into after the washing of washing absorption device in fluorinated tail gas scripture mound
, Jing after circulating cleaning solution two-layer countercurrent washing absorption, the washing of fluorinated tail gas Jing difluoros washing absorption tower is laggard for difluoro washing absorption tower
One stepping enters trifluoro washing absorption tower Jing after three layers of countercurrent washing of circulating cleaning solution absorb, fluorinated tail gas Jing after demister foam removal by
Exhaust fan thrust enters 80m high altitude discharges after the countercurrent washing of three layers of washing tail gas absorption tower absorbs.Wherein washing tail gas absorb
Three layers of countercurrent washing liquid of tower can be returned using gypsum stack according to Wet-process Phosphoric Acid Production operating mode and the switching of exhaust emissions index situation
Water or 10% ammonia.Washing absorption liquid carries out pressure circulated in countercurrent by each circulating pump in each washing absorption equipment.Slag field backwater
Or ammonia is supplemented to washing tail gas absorption tower.As a fluorine scrubbing tower washing absorption liquid (predominantly H2SiF6) solution concentration >=10%
Discharging washing tail gas absorption system afterwards goes hexafluosilicic acid storage tank to settle, as Na after the recovered dissolving iodine therein of supernatant2SiF6Car
Between and anhydrous HF workshop raw material, bottom settle silica gel as white carbon workshop raw material.
This utility model is by having researched and developed Wetting phosphoric acid production washing tail gas absorption plant and method, it is ensured that
Wet-process Phosphoric Acid Production exhaust emissions index (granular material discharged concentration, granular material discharged speed, fluoride emission concentration and fluoride
Rate of discharge) meet《Discharge standard of air pollutants》(GB16297-1996) secondary standard limit value is required.Ensure that
72wt(P2O5The 100%H that the supporting washing tail gas absorption system of)/a wet-process phosphoric acid production plants is produced2SiF6Amount >=1.4wt/a,
100%SiO2Amount about >=2900t/a, washing tail gas absorbing liquid-H2SiF6Solution concentration >=10%.Ensure that Wet-process Phosphoric Acid Production
Washing tail gas absorption system is shut down cleaning cycle >=60d and shuts down clearance time≤1d.Ensure that Wet-process Phosphoric Acid Production tail gas is washed
Wash absorption system and possess coproduction Na2SiF6With anhydrous HF function.Ensure that Wet-process Phosphoric Acid Production washing tail gas absorption system possesses connection
Produce iodine and silicon resource recovery function in tail gas.
This utility model has Wet-process Phosphoric Acid Production washing tail gas assimilation effect substantially, fluorine silicon iodine resource reclaim profit in tail gas
High with rate, plant automation degree is high, the low advantage of operation expense.
Description of the drawings
Fig. 1 is apparatus structure schematic diagram of the present utility model.
Specific embodiment
As shown in figure 1, a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant, including sequentially connecting according to exhaust gas flow direction successively
A fluorine washing absorption tower 1, Venturi scrubbing absorber 2, difluoro washing absorption tower 3, trifluoro washing absorption tower 4 and the tail gas for connecing is washed
Absorption tower 7 is washed, a fluorine washing absorption tower 1 is also connected with hexafluosilicic acid storage tank by hexafluosilicic acid dashpot 8, hexafluosilicic acid pump 9, trifluoro
Demister 5 and blower fan 6 are additionally provided between washing absorption tower 4 and washing tail gas absorption tower 7, demister 5 is configured with demister liquid
Sealing groove 10 and demister cleaning circulation pump.Washing tail gas absorption tower 7 and gypsum stack water return pipeline or 10% ammonia pipeline phase
Even.One fluorine washing absorption tower 1 is provided with two-layer countercurrent spray wash mill and two fluorine spray washing circulating pumps.Difluoro is washed
Absorption tower 3 is provided with two-layer countercurrent spray wash mill and two difluoro spray washing circulating pumps.Trifluoro washing absorption tower 4 is arranged
There are three layers of countercurrent spray wash mill and three trifluoro spray washing circulating pumps.Washing tail gas absorption tower is provided with three layers of adverse current and sprays
Drench wash mill and three tail gas spray washing circulating pumps.Venturi scrubbing absorber 2 is configured with a Venturi scrubbing circulation
Pump.Passed through between washing tail gas absorption tower 7, trifluoro washing absorption tower 4, difluoro washing absorption tower 3 and a fluorine washing absorption tower 1
Flow tube connects.
Embodiment 1
It is 150-200m that gypsum stack backwater amount is mended on washing tail gas absorption tower 73/ h, Jing effusion meters after washing absorption tail gas
Metering, point 10m3/ h sequentially enters tail gas by " 3 → mono- fluorine washing absorption tower 1 of trifluoro 4 → difluoro of washing absorption tower washing absorption tower "
Washing absorption system.Surplus water is pumped up to gypsum stack backwater systemic circulation pond.
All tower body pump inlet pipe two position control butterfly valves are in opening.Sprayed using trifluoro washing absorption tower
Cleaning circulation pump, difluoro washing absorption tower spray washing circulating pump and a fluorine washing absorption tower spray washing circulating pump are respectively to three
Fluorine washing absorption tower 4, difluoro washing absorption tower 3 and a fluorine washing absorption tower 1 carry out excessively stream moisturizing.
(1) to gas-liquid separator liquid seal trough benefit slag field backwater to overfall.
(2) slag field backwater valve Jing effusion meters are opened and measures laggard 7 moisturizing of end of line gas washing absorption tower, when washing tail gas are inhaled
When 7 liquid level of tower is received more than 80%, close 4 washing pump imported valve of trifluoro washing absorption tower, open washing tail gas absorption tower 7 to three
4 excessively stream tube valve of fluorine washing absorption tower, starts correspondence trifluoro washing absorption tower spray washing circulating pump to trifluoro washing absorption tower 4
Carry out moisturizing.
(3) when 4 liquid level of trifluoro washing absorption tower is more than 65%, 3 washing pump imported valve of difluoro washing absorption tower is closed,
Trifluoro washing absorption tower 4 is opened to 3 excessively stream tube valve of difluoro washing absorption tower, starts correspondence difluoro washing absorption tower spray washing
Circulating pump carries out moisturizing to difluoro washing absorption tower 3.
(4) when 3 liquid level of difluoro washing absorption tower is more than 75%, 1 washing pump imported valve of a fluorine washing absorption tower is closed,
3 to one fluorine washing absorption tower of difluoro washing absorption tower, 1 excessively stream tube valve is opened, starts one fluorine washing absorption tower spray washing of correspondence
Circulating pump carries out moisturizing to a fluorine washing absorption tower 1.
(5) when 1 liquid level of a fluorine washing absorption tower reaches 85%, open a fluorine washing absorption tower spray washing circulating pump and enter
Mouth valve, closes 3 to one fluorine washing absorption tower of difluoro washing absorption tower, 1 excessively stream tube valve, starts fluorine washing absorption tower spray
Cleaning circulation pump realizes 1 spray washing of a fluorine washing absorption tower.
(6) difluoro washing absorption tower spray washing circulating pump and venturi spray washing pump inlet valve are opened, is protected
3 liquid level of card difluoro washing absorption tower reaches 80%, closes trifluoro washing absorption tower 4 to 3 excessively stream tube valve of difluoro washing absorption tower,
Start difluoro washing absorption tower spray washing circulating pump and venturi spray washing circulating pump, realize 3 He of difluoro washing absorption tower
2 spray washing of Venturi scrubbing absorber.
(7) open trifluoro washing absorption tower spray washing pump inlet valve, it is ensured that trifluoro washing absorption tower liquid level reaches
To 85%.Washing tail gas absorption tower 7 is closed to 4 excessively stream tube valve of trifluoro washing absorption tower, starts trifluoro washing absorption tower spray
Cleaning circulation pump realizes 4 spray washing of trifluoro washing absorption tower.
(8) washing tail gas absorption tower spray washing pump inlet valve is opened, is started washing tail gas absorption tower spray and is washed
Wash circulating pump and realize 7 spray washing of washing tail gas absorption tower.
(9) when 7 liquid level of washing tail gas absorption tower reaches 85%, start exhaust fan.
(10) when 7 liquid level of washing tail gas absorption tower reaches 90%, open washing tail gas absorption tower spray washing circulating pump
To 4 moisturizing tube valve of trifluoro washing absorption tower, filling pipe valve opening is adjusted, trifluoro washing absorption tower moisturizing flowmeter for pipe stream is made
Amount is shown as 10m3/h。
(11) after 4 liquid level of trifluoro washing absorption tower reaches overflow height, overflow water is with 10m3/ h flows are by " trifluoro is washed
3 → mono- fluorine washing absorption tower 1 of absorption tower 4 → difluoro washing absorption tower " sequentially enters washing tail gas absorption system.
(12) after 1 washing absorption liquid fluorine silicic acid concentration of a fluorine washing absorption tower reaches technology controlling and process index, open a fluorine
Washing absorption tower 1 connects tube valve to hexafluosilicic acid dashpot 8, when 8 liquid level of hexafluosilicic acid dashpot reaches 50%, opens hexafluosilicic acid
9 imported valve of pump, starts hexafluosilicic acid pump 9 and hexafluosilicic acid is pumped into hexafluosilicic acid storage tank.
(13) after 1 washing absorption liquid fluorine silicic acid concentration of a fluorine washing absorption tower reaches technology controlling and process index, open a fluorine
Washing absorption tower 1 connects tube valve to hexafluosilicic acid dashpot 8, after hexafluosilicic acid medial launder liquid level reaches 45% height, starts fluorine
Hexafluosilicic acid is pumped into hexafluosilicic acid storage tank by silicic acid pump 9.After hexafluosilicic acid once settles 10h in hexafluosilicic acid storage tank, start hexafluosilicic acid pump 9
Hexafluosilicic acid finished product is pumped in the depositing reservoir of villiaumite workshop carries out secondary settlement.H after clarification is qualified2SiF6Solution delivers to iodine recovery
Workshop, H2SiF6The operations such as solution is oxidized successively, extraction, absorption, purification, oxidation are obtained essence iodine product.
(14) open hexafluosilicic acid storage tank and tube valve connected to silica gel collecting tank after hexafluosilicic acid transfer sky in hexafluosilicic acid storage tank,
Hexafluosilicic acid storage tank slag field backwater flushing water valve is opened, starts silica gel groove stirring paddle, to reach 50% high when silica gel collecting tank liquid level
After degree, start silica gel pump and silica gel is delivered to into white carbon workshop.
(15) after hexafluosilicic acid groove area geosyncline liquid level reaches 50% height, start geosyncline vertical pump and sewage is pumped into into sewage
Groove, now reduces 7 slag field backwater consumption of washing tail gas absorption tower after Sewage slot liquid level reaches 75% height.Start sewage vertical
Sewage is pumped into trifluoro washing absorption tower 4 by pump.
(16) according to gas-liquid separator fouling condition, periodically open gas-liquid separator cleaning spray tube valve.
Embodiment 2
Washing tail gas absorption tower 7, trifluoro washing absorption tower 4,1 interval of difluoro washing absorption tower 3 and a fluorine washing absorption tower
Formula independence spray washing.Using correspondence trifluoro washing absorption tower spray washing circulating pump excessively stream pipeline, the spray of difluoro washing absorption tower
Cleaning circulation pump excessively stream pipeline and a fluorine washing absorption tower spray washing circulating pump excessively stream pipeline are drenched respectively to trifluoro washing absorption
Tower 4, difluoro washing absorption tower 3 and a fluorine washing absorption tower 1 carry out excessively stream moisturizing.
(1) slag field backwater valve Jing effusion meters are opened and measures laggard 7 moisturizing of end of line gas washing absorption tower, when washing tail gas are inhaled
When 7 liquid level of tower is received more than 90%, open washing tail gas absorption tower 7 to 4 excessively stream tube valve of trifluoro washing absorption tower, start correspondence three
Fluorine washing absorption tower spray washing circulating pump carries out moisturizing to trifluoro washing absorption tower 4.(2) when 4 liquid level of trifluoro washing absorption tower
During more than 80%, trifluoro washing absorption tower 4 is opened to 3 excessively stream tube valve of difluoro washing absorption tower, start correspondence difluoro washing and inhale
Receiving tower spray washing circulating pump carries out moisturizing to difluoro washing absorption tower 3.
(3) when 3 liquid level of difluoro washing absorption tower is more than 80%, open 3 to one fluorine washing absorption of difluoro washing absorption tower
1 excessively stream tube valve of tower, starting one fluorine washing absorption tower spray washing circulating pump of correspondence carries out moisturizing to a fluorine washing absorption tower 1.
(4) when 1 liquid level of a fluorine washing absorption tower is more than 60%, open a fluorine washing absorption tower spray washing circulating pump and enter
Mouth valve, closes 3 to one fluorine washing absorption tower of difluoro washing absorption tower, 1 excessively stream tube valve, starts fluorine washing absorption tower spray
Cleaning circulation pump realizes 1 spray washing of a fluorine washing absorption tower.
(5) difluoro washing absorption tower spray washing circulating pump and venturi spray washing pump inlet valve are opened, is closed
Trifluoro washing absorption tower is closed to difluoro washing absorption tower excessively stream tube valve, start difluoro washing absorption tower spray washing circulating pump and
Venturi spray washing circulating pump, realizes 2 spray washing of difluoro washing absorption tower 3 and Venturi scrubbing absorber.
(6) trifluoro washing absorption tower spray washing pump inlet valve is opened, closes washing tail gas absorption tower 7 to three
4 excessively stream tube valve of fluorine washing absorption tower, starts trifluoro washing absorption tower spray washing circulating pump and realizes that trifluoro washing absorption tower 4 sprays
Drip washing is washed.
(7) washing tail gas absorption tower spray washing pump inlet valve is opened, is started washing tail gas absorption tower spray and is washed
Wash circulating pump and realize 7 spray washing of washing tail gas absorption tower.
(8) after 1 washing absorption liquid fluorine silicic acid concentration of a fluorine washing absorption tower reaches technic index, open fluorine washing and inhale
Receive tower 1 and tube valve is connected to hexafluosilicic acid dashpot 8, when 8 liquid level of hexafluosilicic acid dashpot reaches 30%, open hexafluosilicic acid pump 9 and enter
Mouth valve, starts hexafluosilicic acid pump 9 and hexafluosilicic acid is pumped into hexafluosilicic acid storage tank.
(9) when 1 liquid level of a fluorine washing absorption tower is down to 30%, open 3 to one fluorine washing absorption of difluoro washing absorption tower
1 excessively stream tube valve of tower, carries out moisturizing to a fluorine washing absorption tower 1, when 1 liquid level of a fluorine washing absorption tower reaches 80%, closes
3 to one fluorine washing absorption tower of difluoro washing absorption tower, 1 excessively stream tube valve.
(10) trifluoro washing absorption tower 4 is opened to 3 excessively stream tube valve of difluoro washing absorption tower, to difluoro washing absorption tower 3
Moisturizing is carried out, and when 3 liquid level of difluoro washing absorption tower reaches 80%, trifluoro washing absorption tower 4 is closed to difluoro washing absorption tower 3
Excessively stream tube valve.
(11) washing tail gas absorption tower 7 is opened to 4 excessively stream tube valve of trifluoro washing absorption tower, to trifluoro washing absorption tower 4
Moisturizing is carried out, and when 4 liquid level of trifluoro washing absorption tower reaches 80%, washing tail gas absorption tower 7 is closed to trifluoro washing absorption tower 4
Excessively stream tube valve.
(12) slag field backwater moisturizing tube valve is opened to 7 moisturizing of washing tail gas absorption tower.When 7 liquid level of washing tail gas absorption tower
When reaching 80%, slag field backwater moisturizing tube valve is closed.Hereafter, according to the condition of production, repeat step (6)～(10) behaviour
Make.
(13) after 1 washing absorption liquid fluorine silicic acid concentration of a fluorine washing absorption tower reaches technology controlling and process index, open a fluorine
Washing absorption tower 1 connects tube valve to hexafluosilicic acid dashpot 8, after 8 liquid level of hexafluosilicic acid dashpot reaches 45% height, starts fluorine
Hexafluosilicic acid is pumped into hexafluosilicic acid storage tank by silicic acid pump 9.After in hexafluosilicic acid storage tank, hexafluosilicic acid once settles 10h, after clarification is qualified
H2SiF6Solution delivers to iodine recovery workshop, H2SiF6The operations such as solution is oxidized successively, extraction, absorption, purification, oxidation are obtained essence
Iodine product.
(14) open hexafluosilicic acid storage tank and tube valve connected to silica gel collecting tank after hexafluosilicic acid transfer sky in hexafluosilicic acid storage tank,
Hexafluosilicic acid storage tank slag field backwater flushing water valve is opened, starts silica gel groove stirring paddle, to reach 50% high when silica gel collecting tank liquid level
After degree, start silica gel pump and silica gel is delivered to into white carbon workshop.
(15) after hexafluosilicic acid groove area geosyncline liquid level reaches 50% height, start geosyncline vertical pump and sewage is pumped into into sewage
Groove, now reduces 7 slag field backwater consumption of washing tail gas absorption tower after Sewage slot liquid level reaches 75% height.Start sewage to stand
Sewage is pumped into trifluoro washing absorption tower by formula pump.
(16) according to gas-liquid separator fouling condition, periodically open gas-liquid separator cleaning spray tube valve.
Claims (6)
1. a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant, it is characterised in that：Including sequentially connecting according to exhaust gas flow direction successively
The fluorine washing absorption tower (1) that connects, Venturi scrubbing absorber (2), difluoro washing absorption tower (3), trifluoro washing absorption tower (4)
With washing tail gas absorption tower (7), the fluorine washing absorption tower (1) is also connected with hexafluosilicic acid storage tank, the trifluoro washing absorption
Demister (5) and blower fan (6), the washing tail gas absorption tower (7) are additionally provided between tower (4) and washing tail gas absorption tower (7)
It is connected with gypsum stack water return pipeline or 10% ammonia pipeline.
2. a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant according to claim 1, it is characterised in that：One fluorine
Washing absorption tower (1) is provided with two-layer countercurrent spray wash mill.
3. a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant according to claim 1, it is characterised in that：The difluoro
Washing absorption tower (3) is provided with two-layer countercurrent spray wash mill.
4. a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant according to claim 1, it is characterised in that：The trifluoro
Washing absorption tower (4) is provided with three layers of countercurrent spray wash mill.
5. a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant according to claim 1, it is characterised in that：The tail gas
Washing absorption tower (7) is provided with three layers of countercurrent spray wash mill.
6. a kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant according to claim 1, it is characterised in that：The tail gas
Pass through between washing absorption tower (7), trifluoro washing absorption tower (4), difluoro washing absorption tower (3) and a fluorine washing absorption tower (1)
Flow tube connects.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621014297.8U CN206051573U (en) | 2016-08-31 | 2016-08-31 | A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621014297.8U CN206051573U (en) | 2016-08-31 | 2016-08-31 | A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206051573U true CN206051573U (en) | 2017-03-29 |
Family
ID=58373840
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621014297.8U Expired - Fee Related CN206051573U (en) | 2016-08-31 | 2016-08-31 | A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206051573U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107651781A (en) * | 2017-11-13 | 2018-02-02 | 贵阳开磷化肥有限公司 | Dirty water purification method in a kind of prodan production |
| CN110510591A (en) * | 2019-09-27 | 2019-11-29 | 瓮福达州化工有限责任公司 | A kind of high purity phosphorus hydrochlorate concentration technology |
-
2016
- 2016-08-31 CN CN201621014297.8U patent/CN206051573U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107651781A (en) * | 2017-11-13 | 2018-02-02 | 贵阳开磷化肥有限公司 | Dirty water purification method in a kind of prodan production |
| CN107651781B (en) * | 2017-11-13 | 2020-09-08 | 贵阳开磷化肥有限公司 | Method for purifying sewage in sodium fluosilicate production |
| CN110510591A (en) * | 2019-09-27 | 2019-11-29 | 瓮福达州化工有限责任公司 | A kind of high purity phosphorus hydrochlorate concentration technology |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106268180A (en) | A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant and method | |
| CN103303877B (en) | Many sources of the gas low concentration SO 2smoke comprehensive reclaims acid-making process flow process | |
| CN201959716U (en) | Combination ammonia desulfurization tower | |
| CN104383798A (en) | Flue gas desulfurization and denitration purification recovery system | |
| CN103252158B (en) | Desulfurization system and desulfurization process thereof | |
| CN105797562B (en) | The double ammonia process integration desulfurization denitration systems of coking flue gas two-part | |
| CN205815447U (en) | The double ammonia process integration desulfurization denitration system of coking flue gas two-part | |
| CN206652387U (en) | A kind of ammonia desulfuration equipment of resourcebility | |
| CN105217580B (en) | A kind of method for preparing sulfuric acid with electrolytic manganese residues high temperature desulfurizing enriched flue gas | |
| CN107601434A (en) | A kind of method and apparatus that hydrogen fluoride is prepared by fluosilicic acid | |
| CN105944544A (en) | Petrochemical acidic tail gas treatment system | |
| CN206051573U (en) | A kind of Wet-process Phosphoric Acid Production washing tail gas absorption plant | |
| CN104707459B (en) | Wet magnesium oxide desulphurization electrostatic demisting dust collecting process and equipment | |
| CN210366982U (en) | Absorption device for potassium sulfate byproduct hydrochloric acid by Mannheim method | |
| CN104056538B (en) | Flue gas purifying system and method with integration of desulfurization and denitrification | |
| CN104028083B (en) | A kind of fluorinated tail gas treating apparatus and method | |
| CN206184241U (en) | Full automatically cleaned device of laboratory acid mist waste gas | |
| CN109647137B (en) | Fluorine absorption system for wet-process phosphoric acid | |
| CN205760545U (en) | Three circulating flue gas desulfurization tower or the systems for wet ammonia process desulfurizing | |
| CN104906920A (en) | System for recycling fluorine and silicon resources from wet-process phosphoric acid tail gas and recovery method thereof | |
| CN206372682U (en) | Nitrate method phosphoric acid plant vent gas from reaction tank processing unit | |
| CN206549426U (en) | A kind of chloric acid oxidation flue gas desulfurization, denitrification integrated device | |
| CN101703879A (en) | Aminogroup smoke exhaust purification method and device thereof | |
| CN102614768B (en) | Desulfurization reactor device | |
| CN201454395U (en) | Desulphurization tower combining by using ammonia process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170329 Termination date: 20200831 |