CN106422739A - Calcium-process catalytic cracking flue gas desulfurizing and dedusting system and application - Google Patents
Calcium-process catalytic cracking flue gas desulfurizing and dedusting system and application Download PDFInfo
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- CN106422739A CN106422739A CN201610949070.0A CN201610949070A CN106422739A CN 106422739 A CN106422739 A CN 106422739A CN 201610949070 A CN201610949070 A CN 201610949070A CN 106422739 A CN106422739 A CN 106422739A
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- 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
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Abstract
The invention relates to a calcium-process catalytic cracking flue gas desulfurizing and dedusting system. The system is characterized by comprising a desulfurizing and acidizing tower, an acidizing precipitator, a desulfurizing precipitator, a flocculant storage tank, a first vacuum rotating dewaterer, a wastewater tank, a water collection tank, an oxidization tank, a second gypsum cyclone, a first gypsum cyclone, a vacuum belt dewaterer, an overflowing size tank, a filtrate tank, a lime milk tank and an alkaline liquid tank. Desulfurizing and dedusting of flue gas are integrated in one device (the desulfurizing and acidizing tower), and an acidizing and dedusting section in the desulfurizing and acidizing tower removes the vast majority of catalyst dust and a little amount of SO2 in the flue gas, so that total amount of dust entering a desulfurizing section in the desulfurizing and acidizing tower is reduced, and efficiency desulfurizing and dedusting are realized; solid gypsum can serve as commercial gypsum to be sold, so that economic benefit is increased, and secondary pollution is avoided effectively; by the system, the catalyst dust (hazardous waste) and a gypsum product can be effectively separated, so that wastewater emission of the system is lowered substantially, and running energy consumption and cost are lowered.
Description
Technical field
The invention belongs to environmental technology field, it is related to catalytic cracking flue gas desulfurating dust-removing equipment, especially a kind of calcium method is urged
Change cracking flue gas desulfurization dust-removal system and application.
Background technology
Regeneration fume from catalytic cracking has the characteristics that：In flue gas, ultrafine dust content is high, and dustiness fluctuation is big, temperature wave
Move greatly it is desirable to the continuous cycle of operation of desulphurization system is long.At present, regeneration fume from catalytic cracking desulfurization main technique has：Exxon company
Gas washer (WGS) technique, the EDV wet scrubbing technology of Belco company of U.S. exploitation, the exploitation of Uop Inc.
THIOPAQ bioanalysises, the EP-Absorber method of Lurgi company.The pressure drop of the WGS technique of Exxon company is larger, and upstream is set
Standby safe operation impact is larger, and operating cost is high；The EDV wet scrubbing technology of Belco company of U.S. exploitation, with NaOH or
Soda is desulfurizing agent, and desulfurization product is sodium sulfate.Advantage is to run steadily in the long term, has multiple achievements；Shortcoming is cost
Costliness, operating cost is very high, and wastewater discharge is big, contains the soluble sodium sulfate of high concentration (reaching 12%) in waste water.Uop Inc.
Exploitation THIOPAQ bioanalysises system reliability poor it is impossible to meet the requirement of equipment long-period stable operation.Lurgi is public
The desulfurization degree of the EP-Absorber technology of department is higher, but efficiency of dust collection is not high.
At present, in catalytic cracking flue gas desulfurization and dedusting technology, be most widely used is with Belco company of U.S. EDV
Wet scrubbing technology is the sodium alkali wet desulfurizing process of representative.Catalytic cracking flue gas desulfurization and dedusting system using sodium alkali technique
System wastewater discharge is big, and contains the pollutant such as a large amount of sulphite, sulfate in desulfurization waste liquor, such as without process directly
Discharge can cause serious secondary pollution to environment；And China's desulfurization waste liquor processing cost is very high, a large amount of discharged wastewater met the national standard
Processing cost is higher.And, desulfurization and dedusting is carried out to catalytic cracking flue gas using sodium alkali wet method sulphur removing and dust removing technology, flue gas exists
Contain more flue dust in sweetening process, lead to efficiency of dust collection and desulfuration efficiency to reduce, substantial amounts of efflux wastewater can be produced simultaneously,
And there is the problems such as fouling and blocking, operation expense height occur in desulfurizing tower often and involves great expense.
By retrieval, not yet find the patent publication us related to present patent application.
Content of the invention
It is an object of the invention in place of overcoming the deficiencies in the prior art, providing a kind of calcium method catalytic cracking flue gas desulfurization to remove
Dirt system and application, this system desulfurized effect is good, efficiency of dust collection is high and can effectively realize catalyst dust (danger useless) with
The separation of gypsum product, is greatly reduced system discharge of wastewater, reduces operation energy consumption and cost, prevents desulfurizing tower fouling, blocking etc.
Problem occurs, and this system can be applied in flue gas desulfurization and dedusting.
The purpose of the present invention is achieved through the following technical solutions：
A kind of calcium method catalytic cracking flue gas desulfurization dust-removal system, described system includes desulfation tower, acid precipitation device, takes off
Sulfur depositor, flocculant storage tank, 1# vacuum rotating dewaterer, waste water tank, header tank, oxidation tank, 2# Gypsum Fibrosum cyclone, 1# Gypsum Fibrosum
Cyclone, vacuum belt dewaterer, overflow slurry tank, filtrate box, lime white tank and lye tank；
From top to bottom it is interval with exhanst gas outlet, demister, desulfurization section and acidifying dedusting successively in described desulfation tower
Section, described acidifying dedusting section includes being acidified spray section, Pneumatic desulphurization dust removing units and interval are located at acidifying spray section and pneumatic de-
Acidifying storage slurry section below sulfur dust removing units, the desulfation tower between described acidifying spray section and acidifying storage slurry section is connected
It is provided with smoke inlet, described desulfurization section includes desulfurization spray section, Pneumatic desulfuration unit and interval and is located at desulfurization spray section and pneumatic
Desulfurization storage slurry section below desulfurization unit；
The bottom of described acidifying storage slurry section is connected with the input of acid precipitation device by acidifying dedusting section slurry pump and sets
Put, the input of acid precipitation device is connected with the outfan of flocculant storage tank setting also by flocculant dosing pump, acidifying is heavy
The supernatant outfan of shallow lake device is connected setting with acidifying storage slurry section, the bottom high concentrate dust serosity outfan of acid precipitation device
Be connected setting with the input of desulfurization depositor, the input of the bottom outfan of desulfurization depositor and 1# vacuum rotating dewaterer
End is connected setting, the filtrate outfan of this 1# vacuum rotating dewaterer respectively with the input of waste water tank, acid precipitation device
Input is connected setting, and the dust filter cake outfan of 1# vacuum rotating dewaterer is connected with outward transport vehicle setting, described gives up
The outfan of water tank passes through waste water tank slurry pump to efflux wastewater；
The outfan of described header tank passes through water collecting pump and the setting that is connected in smoke inlet；
The bottom of described desulfurization storage slurry section is connected with the input of oxidation tank setting, and the concentration of slurry of oxidation tank is less than
15%～18% serosity outfan is connected with the input of 2# Gypsum Fibrosum cyclone setting by 2# oxidation tank slurry pump, this 2#
The concentration that Gypsum Fibrosum cyclone can be less than 15%～18% serosity to concentration of slurry in oxidation tank carries out thickening, this 2# Gypsum Fibrosum eddy flow
The underflow high concentration serosity outfan of device is connected with oxidation tank setting, the overflow low concentration serosity output of this 2# Gypsum Fibrosum cyclone
End by slurry distribution box respectively with the setting that is connected in the input of overflow slurry tank, oxidation tank, described overflow slurry tank
Serosity outfan is returned pump by desulfurization section and is connected with desulfurization spray section setting；
The bottom Gypsum Fibrosum outfan of described oxidation tank passes through the input phase of 1# oxidation tank slurry pump and 1# Gypsum Fibrosum cyclone
Connect setting, the underflow outfan of described 1# Gypsum Fibrosum cyclone is connected with the input of vacuum belt dewaterer setting, vacuum
The outfan of belt dewaterer includes solid Gypsum Fibrosum outfan and filtrate outfan, and described solid Gypsum Fibrosum outfan can export solid
Body Gypsum Fibrosum, described filtrate outfan is passed sequentially through vacuum pump, steam-water separator and is connected with the input of filtrate box setting；Described
The overflow outfan of 1# Gypsum Fibrosum cyclone passes through slurry distribution box and sets with being connected in the input of filtrate box, oxidation tank respectively
Put；
The outfan of described filtrate box is connected with the input of lime white tank, acid precipitation device respectively by filtrate pump and sets
Put, the outfan of described lime white tank is connected with desulfurization spray section setting by milk of lime pump, setting stone in this lime white tank
Grey whey liquid；
The outfan of described lye tank passes through lye pump and the setting that is connected in waste water tank, and the outfan of this lye tank also leads to
Cross lye pump, 3# circulating pump, 4# circulating pump and acidifying spray section to be connected setting；
The discharge duct of described waste water tank and the discharge duct of oxidation tank are all connected with smoke inlet setting.
And, described acidifying dedusting section is pneumatic dust collection section, and described desulfurization section is Pneumatic desulphurization section；Or, described acidifying
The bottom vertical height of depositor is higher than the top vertical height of acidifying storage slurry section；Or, the input of described desulfurization depositor
It is disposed in proximity at the bottom of desulfurization depositor；Or, described alkali liquor is NaOH solution.
And, the pH value of the souring soln in described acidifying dedusting section maintains between 3.0～5.0；Or, described desulfurization
The bottom vertical height of storage slurry section is higher than the top vertical height of the input of oxidation tank.
And, the pH value of the serosity in described oxidation tank controls between 5.0～6.0；Or, de- in described desulfurization section
The pH value of sulfur serosity maintains between 5.0～7.0；Or, described lime milk liquid energy enough makes the pH value of serosity in desulfurization section tie up
Hold between 5.0～7.0.
And, the forming step of described solid Gypsum Fibrosum is：When in oxidation tank, concentration of slurry is higher than that 15%～18%, pH value exists
When between 5.0～6.0, the calcium sulfite in serosity in oxidation tank generates larger gypsum crystal through oxidizing and crystallizing, then carries out
Thickening generates the solid Gypsum Fibrosum of high-purity low-water-content.
And, described desulfurization spray section includes spaced upper desulfurization spray section and lower desulfurization spray section, described desulfurization
Section Pneumatic desulfuration unit be arranged between desulfurization spray section and lower desulfurization spray section, described system also include 1# circulating pump and
2# circulating pump, the input of described 1# circulating pump and desulfurization are store slurry section and are connected setting, and the outfan of this 1# circulating pump is taken off with upper
Sulfur spray section is connected setting, and the input of this 1# circulating pump also returns the outfan phase of pump respectively with milk of lime pump, desulfurization section
Connect setting, the input of described 2# circulating pump and desulfurization are store slurry section and are connected setting, and the outfan of this 2# circulating pump is taken off with lower
Sulfur spray section is connected setting.
And, described acidifying spray section includes spaced upper acidifying spray section and lower acidifying spray section, described acidifying
The Pneumatic desulphurization dust removing units of dedusting section are arranged between acidifying spray section and lower acidifying spray section, and described system also includes 3#
Circulating pump and 4# circulating pump, the input of described 3# circulating pump is connected setting with acidifying storage slurry section, the output of this 3# circulating pump
End is connected setting with the upper spray section that is acidified, and the input of this 3# circulating pump is also connected with the outfan of lye pump setting, institute
State the input of 4# circulating pump and acidifying storage slurry section is connected setting, the outfan of this 4# circulating pump is connected with the lower spray section that is acidified
Connect setting, the input of this 4# circulating pump is also connected with the outfan of lye pump setting.
And, described system also includes post processing zone melt pit and sump pump, is provided with melt pit serosity in this post processing zone melt pit,
The outfan of described post processing zone melt pit passes through sump pump and the setting that is connected in oxidation tank.
And, described oxidation tank is also connected with roots blower setting, the outfan of roots blower be arranged at oxidation tank
The aerating pipelines of inner bottom part are connected setting；Described waste water tank is also connected with compressed air cylinder setting, compressed air cylinder defeated
Go out and hold the setting that is connected with the aerating pipelines being arranged at waste water tank inner bottom part.
Application during calcium method catalytic cracking flue gas desulfurization dust-removal system is in terms of flue gas desulfurization and dedusting as above.
The advantage that the present invention obtains and good effect are：
1st, this desulfurization dust-removal system is provided with desulfation tower, acid precipitation device, desulfurization depositor, flocculant storage tank, 1#
Vacuum rotating dewaterer, waste water tank, header tank, oxidation tank, 2# Gypsum Fibrosum cyclone, 1# Gypsum Fibrosum cyclone, vacuum belt dewaterer,
Overflow slurry tank, filtrate box, lime white tank and lye tank, according to aerodynamic principle, install pneumatic in acidifying dedusting section
Desulfurization and dedusting unit, acidifying spray section etc., most catalyst dusts and a small amount of SO in removing flue gas2, reduce catalyst powder
Dirt enters the total amount of desulfurization section, and acidified slurries enter acid precipitation device, and the dust precipitating enters 1# together with desulfurization dust
The abjection outward transport of vacuum rotating dewaterer；Desulfurization section and the lime white tank equipped with lime cream serosity etc. are connected, using lime milk
Liquid carries out desulfurization and dedusting, so that lime cream serosity and flue gas is fully contacted by desulfurization spray section and Pneumatic desulfuration unit, realizes high
Effect desulfurization and dedusting；Solid Gypsum Fibrosum after vacuum belt dewaterer is processed exports through solid Gypsum Fibrosum outfan, can be used as business stone
Cream is sold, and had both improve economic benefit, and efficiently avoid secondary pollution again；Meanwhile, this system can be effectively realized catalyst
Dust (danger is useless) is separated with gypsum product, system discharge of wastewater is greatly reduced, reduces operation energy consumption and cost；This system desulfurization
Acidifying tower desulfurized effect is good, efficiency of dust collection is high, SO in exiting flue gas2Concentration is less than 35mg/Nm3, dust concentration be less than 5mg/Nm3.
2nd, the desulfurization of flue gas, dedusting are integrated in a device desulfation tower by the desulfation tower of the system setting
In carry out, the desulfurization section in desulfation tower is substantially carried out flue gas desulfurization, and acidifying dedusting section is substantially carried out flue gas ash removal, and existing
In technology, other catalytic cracking unit flue gas dust collecting systems mainly pass through cleaner (the general employing of setting before desulfurizer
Dry electric precipitation device) carry out dedusting, flue gas enters back into desulfurizer after dedusting and carries out desulfurization, i.e. flue gas desulfurization device and removing
Dirt device is provided separately.Compared to other catalytic cracking flue gas desulfurization dust-removal systems, which system reduces construction cost and operation
Energy consumption, decreases floor space.
3rd, the overflow slurry tank of the system, to flow the overflow slurry for 2# Gypsum Fibrosum cyclone, returns pump pumping by desulfurization section
To desulfurization section, continue cycling through participation desulphurization reaction, and desulfurization section interior circulation serum density can be effectively reduced, prevent in tower
Deposition and the generation of fouling.
4th, the waste water tank of the system is connected with lye tank setting, and waste water tank is also connected with compressed air cylinder setting, pressure
The outfan of contracting air tank is connected with the aerating pipelines being arranged at waste water tank inner bottom part setting, and the effect of this compressed air cylinder is
There is provided oxidation air into waste water tank, after oxidation air is passed through waste water tank, be fully contacted with waste water in the presence of aerating pipelines,
Reduce the COD content in waste water, in waste water tank, be passed through aerating pipelines, increase NaOH solution pipeline, in the wastewater flow rate needing outer row
Arrange outward again after regulation is up to standard, it is possible to reduce the pollution to environment；In addition, the discharge duct of the discharge duct of waste water tank and oxidation tank
All it is connected setting with smoke inlet so that the discharge gas discharging gas and oxidation tank in waste water tank all can enter flue gas and enter
Mouth, it is ensured that the waste water tank after sealed process and oxidation tank body air pressure balance, carries out desulfurization and dedusting to discharge gas simultaneously again,
Prevent air pollution.
5th, the system is provided with oxidation tank, and the oxidizing and crystallizing of calcium sulfite can be carried out in oxidation tank, oxidation tank entoplasm
Liquid pH value controls between 5.0～6.0, is conducive to the complete oxidation of calcium sulfite, significantly improves desulfuration byproduct Gypsum Fibrosum
Purity, after vacuum belt dewaterer processed, the solid Gypsum Fibrosum moisture content of generation is less than 10%, Ca (OH)2Content is little
In 2%, the Cl content being dissolved in Gypsum Fibrosum is less than 100ppm, can sell as business Gypsum Fibrosum.
6th, in the acidifying dedusting section of the system, dedusting is carried out using spray section and pneumatic desulfurization and dedusting unit, smoke abatement can be removed
Most of flue dust in gas, then through the further dedusting of desulfurization section so that the efficiency of dust collection of desulfation tower greatly improves, desulfurization
Acidifying tower outlet dust concentration is less than 5mg/Nm3.
7th, the system makes lime cream serosity and flue gas be fully contacted by desulfurization spray section and Pneumatic desulfuration unit, and desulfurization is imitated
Rate is high, SO in desulfation tower exiting flue gas2Concentration is less than 35mg/Nm3.
8th, desulfation tower is connected with exhanst gas outlet and is set together, unites two into one by the system, significantly reduces
Building cost and floor space.
9th, the acidifying dedusting section of the system be arranged at former flue gas before desulfurization section so that former flue gas with acidifying dedusting section
First contacted, using the SO in flue gas2Solution is acidified, has saved cost.
10th, the oxidation tank of the system is also connected with roots blower setting, the outfan of roots blower be arranged at oxidation
The aerating pipelines of tank inner bottom part are connected setting, and the effect of this roots blower is the offer oxidation air into oxidation tank, and oxidation is empty
After gas is passed through oxidation tank, it is fully contacted with serosity in the presence of aerating pipelines, make the sulfurous in the oxygen and serosity of in the air
Sour calcium reaction generates calcium sulfate.
Brief description
Fig. 1 is the structure connection diagram of present system.
Specific embodiment
Below in conjunction with the accompanying drawings and by embodiment, the present invention is further elaborated, and the following example is illustrative
, be not determinate it is impossible to following described limiting protection scope of the present invention.
The structure that do not describe in detail in the present invention, annexation etc. are it can be understood as ordinary skill in the art means.
A kind of calcium method catalytic cracking flue gas desulfurization dust-removal system, as shown in figure 1, described system includes desulfation tower, acid
Change depositor, desulfurization depositor, flocculant storage tank, 1# vacuum rotating dewaterer, waste water tank, header tank, oxidation tank, the rotation of 2# Gypsum Fibrosum
Stream device, 1# Gypsum Fibrosum cyclone, vacuum belt dewaterer, overflow slurry tank, filtrate box, lime white tank and lye tank；
From top to bottom it is interval with exhanst gas outlet 1, demister 2, desulfurization section and acidifying in described desulfation tower successively to remove
Dirt section, it is gentle that described acidifying dedusting section includes being acidified spray section 6, Pneumatic desulphurization dust removing units 7 and interval are located at acidifying spray section
Acidifying storage slurry section 9 below dynamic desulfurization and dedusting unit, on the desulfation tower between described acidifying spray section and acidifying storage slurry section
It is connected and is provided with smoke inlet 8, described desulfurization section includes desulfurization spray section 3, Pneumatic desulfuration unit 4 and interval and is located at desulfurization spray
Desulfurization storage slurry section 5 below section and Pneumatic desulfuration unit；Especially, the desulfurization of flue gas, dedusting are integrated in a dress by the system
Put in (desulfation tower) and carry out, the desulfurization section in desulfation tower is substantially carried out flue gas desulfurization, acidifying dedusting section is substantially carried out
Flue gas ash removal, described acidifying dedusting section is mainly pneumatic dust collection section, and described desulfurization section is mainly Pneumatic desulphurization section；More preferably, institute
The pH value stating the souring soln in acidifying dedusting section maintains between 3.0～5.0；
The bottom of described acidifying storage slurry section is connected with the input of acid precipitation device by acidifying dedusting section slurry pump and sets
Put, the input of acid precipitation device is connected with the outfan of flocculant storage tank setting also by flocculant dosing pump, acidifying is heavy
The supernatant outfan of shallow lake device is connected setting, more preferably, the bottom vertical height of described acid precipitation device with acidifying storage slurry section
Top vertical height, the bottom high concentrate dust serosity outfan of acid precipitation device and desulfurization depositor higher than acidifying storage slurry section
Input (more preferably, the input of described desulfurization depositor is disposed in proximity at the bottom of desulfurization depositor) being connected sets
Put, the bottom outfan of desulfurization depositor is connected with the input of 1# vacuum rotating dewaterer setting, this 1# vacuum rotating takes off
The filtrate outfan of water dispenser is connected with the input of waste water tank, the input of acid precipitation device setting respectively, and filtrate is used for giving up
Arrange or reenter acid precipitation device outside water and carry out secondary precipitation, the dust filter cake outfan (in figure of 1# vacuum rotating dewaterer
Non- label) it is connected setting with outward transport vehicle, dust filter cake can be by transporting outward vehicle outward transport, and the outfan of described waste water tank is logical
Cross waste water tank slurry pump to efflux wastewater；
In acidifying storage slurry section, the portion of water in solution is fallen by smoke evaporative, and remaining solution is by being acidified dedusting section plasma discharge
It is pumped into acid precipitation device, pass through flocculant dosing pump simultaneously and add flocculation from flocculant storage tank in acid precipitation device
Catalyst dust, in the presence of flocculant, is precipitated by agent by gravitational settling, and after precipitation, supernatant flows back to (example
As certainly flowed back to) it is acidified storage slurry section interior circulation use, acid precipitation device bottom high concentrate dust serosity is delivered in desulfurization depositor
(more preferably, being delivered to the near-bottom of desulfurization depositor), then enters 1# vacuum rotating dewaterer together with desulfurization dust, filter
Liquid goes waste water tank to be used for outside waste water arranging or reenter acid precipitation device and carry out secondary precipitation, and dust filter cake is then passed through outside vehicle
Fortune；
The outfan of described header tank passes through water collecting pump and the setting that is connected in smoke inlet, this header tank and water collecting pump
Setting is so that the supplementary water in acidifying dedusting section timely can be supplied by the water in header tank；
The bottom of described desulfurization storage slurry section is connected with the input of oxidation tank setting, and more preferably, described desulfurization is store and starched section
Bottom vertical height be higher than oxidation tank input top vertical height, the concentration of slurry of oxidation tank is less than 15%～18%
Serosity outfan be connected with the input of 2# Gypsum Fibrosum cyclone setting by 2# oxidation tank slurry pump, this 2# Gypsum Fibrosum cyclone
The concentration being less than 15%～18% serosity to concentration of slurry in oxidation tank carries out thickening, the underflow high concentration of this 2# Gypsum Fibrosum cyclone
Serosity outfan is connected with oxidation tank setting, and the overflow low concentration serosity outfan of this 2# Gypsum Fibrosum cyclone passes through distribution of slurry
Case respectively with the setting that is connected in the input of overflow slurry tank, oxidation tank, the serosity outfan of described overflow slurry tank passes through
Desulfurization section is returned pump and is connected with desulfurization spray section setting；More preferably, the pH value of the serosity in described oxidation tank control 5.0～
6.0 between；More preferably, the pH value of the desulfurization slurry in described desulfurization section maintains between 5.0～7.0；
The bottom Gypsum Fibrosum outfan of described oxidation tank passes through the input phase of 1# oxidation tank slurry pump and 1# Gypsum Fibrosum cyclone
Connect setting, the underflow outfan of described 1# Gypsum Fibrosum cyclone is connected with the input of vacuum belt dewaterer setting, vacuum
The outfan of belt dewaterer includes solid Gypsum Fibrosum outfan and filtrate outfan (the non-label of in figure), described solid Gypsum Fibrosum output
End can export solid Gypsum Fibrosum, and described filtrate outfan passes sequentially through the input phase of vacuum pump, steam-water separator and filtrate box
Connect setting；The overflow outfan of described 1# Gypsum Fibrosum cyclone passes through slurry distribution box input, the oxidation with filtrate box respectively
Be connected in tank setting；
The outfan of described filtrate box is connected with the input of lime white tank, acid precipitation device respectively by filtrate pump and sets
Put, the outfan of described lime white tank is connected with desulfurization spray section setting by milk of lime pump, setting stone in this lime white tank
Grey whey liquid, lime milk liquid energy enough makes the pH value of serosity in desulfurization section maintain between 5.0～7.0；
Serosity (more preferably, flowing automatically) in described desulfurization storage slurry section enters oxidation tank, and in oxidation tank, concentration of slurry is less than
When 15%～18%, the serosity outfan being less than 15%～18% from concentration of slurry is pumped to 2# stone by 2# oxidation tank slurry pump
Cream cyclone, the concentration that 2# Gypsum Fibrosum cyclone is less than 15%～18% serosity to the concentration of slurry in oxidation tank carries out thickening, 2#
Gypsum Fibrosum cyclone underflow high concentration serosity returns oxidation tank, the overflow of 2# Gypsum Fibrosum cyclone by underflow high concentration serosity outfan
Low concentration serosity is delivered in overflow slurry tank by slurry distribution box or is returned in oxidation tank, and overflow slurry tank serosity is through fully
Return pump by desulfurization section again after stirring to be back in desulfurization section；In oxidation tank, concentration of slurry is higher than 15%～18%, pH value
(when slurry pH value is low, part melt pit serosity can be squeezed into and be adjusted), in serosity when controlling between 5.0～6.0
Calcium sulfite generates calcium sulfate through peroxidating, and calcium sulfate, in oxidation tank intercrystalline, generates Gypsum Fibrosum, after gypsum crystal is grown up,
Pump into 1# Gypsum Fibrosum cyclone by 1# oxidation tank slurry pump to be concentrated, the underflow of 1# Gypsum Fibrosum cyclone enters vacuum belt dehydration
After machine dehydration, generate moisture content and be less than 10%, Ca (OH)2Content is less than 2%, and the Cl content being dissolved in Gypsum Fibrosum is less than 100ppm
Solid Gypsum Fibrosum, exported by solid Gypsum Fibrosum outfan, the overflow of 1# Gypsum Fibrosum cyclone delivers to filtrate box by slurry distribution box
Interior or return oxidation tank in.Enter the overflow of 1# Gypsum Fibrosum cyclone, vacuum belt dewaterer and the steam-water separator of filtrate box
Filtrate is delivered in lime white tank through filtrate pump and is used for slurrying, is delivered to lime milk liquid pump in desulfurization section by milk of lime pump
Participation desulphurization reaction, and the pH value of serosity in tower can be improved, so that the pH value of serosity in desulfurization section is maintained between 5.0～7.0.
Meanwhile, the outfan of filtrate box is connected with the input of acid precipitation device setting by filtrate pump, will be outer after desulfurization process
Effluent is pumped to acid precipitation device by filtrate pump, through precipitation after with acidification after efflux wastewater amount converge after by 1#
Vacuum rotating dewaterer filtrate is pumped to the qualified rear outer row of waste water tank aerating regulation；
The outfan of described lye tank passes through lye pump and the setting that is connected in waste water tank, and the outfan of this lye tank also leads to
Cross lye pump, 3# circulating pump, 4# circulating pump and acidifying spray section to be connected setting；The lye export of the outfan of lye tank is gone to
Two-way direction, includes the pH value that waste water tank adjusts efflux wastewater respectively, goes to be acidified in adjustment acidifying dedusting section in spray section
The pH value of serosity；In the present embodiment, described alkali liquor is NaOH solution；
The discharge duct of described waste water tank is all connected with smoke inlet with the discharge duct of oxidation tank, and (in figure is not shown for setting
Go out) so that the discharge gas discharging gas and oxidation tank in waste water tank all can enter smoke inlet it is ensured that after sealed process
Waste water tank and oxidation tank body air pressure balance, simultaneously again to discharge gas carry out desulfurization and dedusting, prevent air pollution.
It is true that this desulfurization dust-removal system is provided with desulfation tower, acid precipitation device, desulfurization depositor, flocculant storage tank, 1#
Empty rotary dewaterer, waste water tank, header tank, oxidation tank, 2# Gypsum Fibrosum cyclone, 1# Gypsum Fibrosum cyclone, vacuum belt dewaterer, overflow
Stream serum pot, filtrate box, lime white tank and lye tank, according to aerodynamic principle, install pneumatic de- in acidifying dedusting section
Sulfur dust removing units, acidifying spray section etc., most catalyst dusts and a small amount of SO in removing flue gas2, reduce catalyst dust
Enter the total amount of desulfurization section, acidified slurries enter acid precipitation device, and it is true that the dust precipitating enters 1# together with desulfurization dust
Empty rotary dewaterer abjection outward transport；Desulfurization section and the lime white tank equipped with lime cream serosity etc. are connected, using lime cream serosity
Carry out desulfurization and dedusting, so that lime cream serosity and flue gas is fully contacted by desulfurization spray section and Pneumatic desulfuration unit, realize efficiently
Desulfurization and dedusting；Solid Gypsum Fibrosum after vacuum belt dewaterer is processed exports through solid Gypsum Fibrosum outfan, can be used as business Gypsum Fibrosum
Sell, both improve economic benefit, and efficiently avoid secondary pollution again；Meanwhile, this system can be effectively realized catalyst powder
Dirt (danger is useless) is separated with gypsum product, system discharge of wastewater is greatly reduced, reduces operation energy consumption and cost.
The desulfurization of flue gas, dedusting are integrated in a device desulfation tower desulfation tower of the system setting
Carry out, the desulfurization section in desulfation tower is substantially carried out flue gas desulfurization, and acidifying dedusting section is substantially carried out flue gas ash removal, and existing skill
In art, other catalytic cracking unit flue gas dust collecting systems mainly pass through the cleaner of setting before desulfurizer (typically using dry
Formula electric cleaner) carry out dedusting, flue gas enters back into desulfurizer after dedusting and carries out desulfurization, i.e. flue gas desulfurization device and dedusting
Device is provided separately.Compared to other catalytic cracking flue gas desulfurization dust-removal systems, which system reduces construction cost and run energy
Consumption, decreases floor space.
In the present embodiment, described desulfurization spray section includes spaced upper desulfurization spray section and lower desulfurization spray section
(the non-label of in figure), the Pneumatic desulfuration unit of described desulfurization section is arranged between desulfurization spray section and lower desulfurization spray section, institute
System of stating also includes 1# circulating pump and 2# circulating pump, and the input of described 1# circulating pump and desulfurization are store slurry section and be connected setting, this
The outfan of 1# circulating pump is connected with upper desulfurization spray section setting, the input of this 1# circulating pump also respectively with milk of lime pump,
The outfan that desulfurization section returns pump is connected setting, and the input of described 2# circulating pump and desulfurization storage are starched section and be connected setting, this
The outfan of 2# circulating pump is connected with lower desulfurization spray section setting.The system is provided with 1# circulating pump and 2# circulating pump, and 1# follows
Desulfurization can be store serosity in slurry section and be returned, with the desulfurization section of overflow slurry tank, the overflow slurry tank low concentration that pumping comes by ring pump
The lime cream serosity of serosity and milk of lime pump pumping is together got in desulfurization spray section, provides desulfurization slurry for Pneumatic desulfuration unit
Liquid, improves desulfurized effect, also saves resource.
In the present embodiment, described acidifying spray section includes spaced upper acidifying spray section and lower acidifying spray section
(the non-label of in figure), the Pneumatic desulphurization dust removing units of described acidifying dedusting section are arranged at acidifying spray section and lower acidifying spray section
Between, described system also includes 3# circulating pump and 4# circulating pump, and the input of described 3# circulating pump is connected with acidifying storage slurry section
Setting, the outfan of this 3# circulating pump is connected setting with the upper spray section that is acidified, the input of this 3# circulating pump also with lye pump
Outfan be connected setting, the input of described 4# circulating pump is connected with acidifying storage slurry section setting, this 4# circulating pump defeated
Go out end to be connected setting with the lower spray section that is acidified, the input of this 4# circulating pump is also connected with the outfan of lye pump setting.
The system is provided with 3# circulating pump and 4# circulating pump, 3# circulating pump and 4# circulating pump can by serosity in acidifying storage slurry section with
The alkali liquor that lye pump pumping comes together is got in acidifying spray section, provides acidified slurries for acidifying unit, improves acidizing effect,
Also save resource.
In the present embodiment, described system also includes post processing zone melt pit and sump pump, is provided with this post processing zone melt pit
Melt pit serosity, the outfan of described post processing zone melt pit passes through sump pump and the setting that is connected in oxidation tank.When oxidation tank entoplasm
When liquid concentration is higher than that 15%～18%, pH value controls between 5.0～6.0, the calcium sulfite in serosity generates sulfur through peroxidating
Sour calcium, calcium sulfate, in oxidation tank intercrystalline, generates Gypsum Fibrosum, after gypsum crystal is grown up, you can discharge, when the slurry in oxidation tank
During liquid pH value low (between 5.0～6.0), squeezed in the melt pit of post processing zone partly into oxidation tank by sump pump
Hole serosity is adjusted the slurry pH value in oxidation tank.
In the present embodiment, described oxidation tank is also connected with roots blower setting, the outfan of roots blower and setting
Aerating pipelines 10 in oxidation tank inner bottom part are connected setting, and the effect of this roots blower is to provide oxidation empty into oxidation tank
Gas, after oxidation air is passed through oxidation tank, is fully contacted with serosity in the presence of aerating pipelines, makes oxygen and the serosity of in the air
In calcium sulfite reaction generate calcium sulfate；Described waste water tank is also connected with compressed air cylinder setting, compressed air cylinder defeated
Go out and hold the setting that is connected with the aerating pipelines being arranged at waste water tank inner bottom part, the effect of this compressed air cylinder is to carry into waste water tank
For oxidation air, after oxidation air is passed through waste water tank, it is fully contacted with waste water in the presence of aerating pipelines, reduce in waste water
COD content.
Operation principle one kind of the system can be understood as：
The system includes desulfurization section, acidifying dedusting section, acid precipitation device, desulfurization depositor, waste water tank, lye tank, overflow
The equipment such as serum pot, oxidation tank, filtrate box, after former flue gas is entered in desulfation tower by smoke inlet, in acidifying dedusting section
Desulfurization and dedusting is carried out for absorbent with souring soln to former flue gas, absorbs most catalyst dusts and small part in flue gas
SO2, in desulfurization section, desulfurization and dedusting is carried out for desulfurizing agent with lime cream serosity, in desulfurization section, flue gas and lime cream serosity fully connect
Touch, most of SO in removing flue gas2, one-step removal exhaust gas dust of going forward side by side；
In storage slurry section in acidifying dedusting section, the portion of water in solution is fallen by smoke evaporative, and remaining solution is removed by being acidified
Dirt section plasma discharge is pumped into acid precipitation device, in the presence of flocculant, by gravitational settling, catalyst dust is precipitated,
After precipitation, acid precipitation device bottom high concentrate dust serosity is delivered to desulfurization depositor near-bottom, then with desulfurized powder
Dirt enters vacuum rotating dewaterer together, to remove solid dust impurity；Acidifying dedusting section is supplemented water and is derived from header tank by collection
The flushing water at smoke inlet delivered to by water pump；
Serosity after desulfurization and dedusting is mainly calcium sulfite solution and solid precipitation impurity, and flue gas passes through desulfation tower and takes off
After sulfur dedusting, neat stress enters the exhanst gas outlet of tower top after demister removes the droplet carried secretly in air-flow, then directly arranges
Enter air, to realize nicotinic acids；
Desulfurization slurry gravity flow enters oxidation tank, when in oxidation tank, concentration of slurry is less than 15%～18%, by oxidation tank
Serosity is pumped to Gypsum Fibrosum cyclone by slurry pump, and Gypsum Fibrosum cyclone underflow high concentration serosity returns oxidation tank, to realize to oxidation
In tank, concentration of slurry carries out thickening；Concentration of slurry in oxidation tank be higher than 15%～18%, pH value between 5.0～6.0 when, oxygen
The calcium sulfite changed in serosity in tank generates larger gypsum crystal through oxidizing and crystallizing, then carries out thickening generation high-purity
The solid Gypsum Fibrosum of low-water-content.
Claims (10)
1. a kind of calcium method catalytic cracking flue gas desulfurization dust-removal system it is characterised in that：Described system includes desulfation tower, acidifying
Depositor, desulfurization depositor, flocculant storage tank, 1# vacuum rotating dewaterer, waste water tank, header tank, oxidation tank, 2# Gypsum Fibrosum eddy flow
Device, 1# Gypsum Fibrosum cyclone, vacuum belt dewaterer, overflow slurry tank, filtrate box, lime white tank and lye tank；
From top to bottom it is interval with exhanst gas outlet, demister, desulfurization section and acidifying dedusting section, institute successively in described desulfation tower
State that acidifying dedusting section includes being acidified spray section, Pneumatic desulphurization dust removing units and interval are located at acidifying spray section and pneumatic desulfurization and dedusting
Acidifying storage slurry section below unit, the desulfation tower between described acidifying spray section and acidifying storage slurry section is connected and is provided with cigarette
Gas entrance, described desulfurization section includes desulfurization spray section, Pneumatic desulfuration unit and interval and is located at desulfurization spray section and Pneumatic desulphurization list
The desulfurization storage slurry section of unit lower section；
The bottom of described acidifying storage slurry section is passed through to be acidified dedusting section slurry pump and is connected with the input of acid precipitation device setting, sour
The input changing depositor is connected with the outfan of flocculant storage tank setting also by flocculant dosing pump, acid precipitation device
Supernatant outfan is connected setting, the bottom high concentrate dust serosity outfan of acid precipitation device and desulfurization with acidifying storage slurry section
The input of depositor is connected setting, and the bottom outfan of desulfurization depositor is connected with the input of 1# vacuum rotating dewaterer
Connect setting, the filtrate outfan of this 1# vacuum rotating dewaterer input with the input of waste water tank, acid precipitation device respectively
Be connected setting, and the dust filter cake outfan of 1# vacuum rotating dewaterer is connected setting with outward transport vehicle, described waste water tank
Outfan passes through waste water tank slurry pump to efflux wastewater；
The outfan of described header tank passes through water collecting pump and the setting that is connected in smoke inlet；
The bottom of described desulfurization storage slurry section is connected with the input of oxidation tank setting, the concentration of slurry of oxidation tank less than 15%～
18% serosity outfan is connected with the input of 2# Gypsum Fibrosum cyclone setting by 2# oxidation tank slurry pump, and this 2# Gypsum Fibrosum revolves
The concentration that stream device can be less than 15%～18% serosity to concentration of slurry in oxidation tank carries out thickening, the bottom of this 2# Gypsum Fibrosum cyclone
Stream high concentration serosity outfan is connected with oxidation tank setting, and the overflow low concentration serosity outfan of this 2# Gypsum Fibrosum cyclone passes through
Slurry distribution box respectively with the setting that is connected in the input of overflow slurry tank, oxidation tank, the serosity of described overflow slurry tank is defeated
Go out end to be connected with desulfurization spray section setting by desulfurization section return pump；
The bottom Gypsum Fibrosum outfan of described oxidation tank is connected with the input of 1# Gypsum Fibrosum cyclone by 1# oxidation tank slurry pump
Setting, the underflow outfan of described 1# Gypsum Fibrosum cyclone is connected with the input of vacuum belt dewaterer setting, vacuum belt
The outfan of dewaterer includes solid Gypsum Fibrosum outfan and filtrate outfan, and described solid Gypsum Fibrosum outfan can export solid stone
Cream, described filtrate outfan is passed sequentially through vacuum pump, steam-water separator and is connected with the input of filtrate box setting；Described 1# stone
The overflow outfan of cream cyclone pass through slurry distribution box respectively with the setting that is connected in the input of filtrate box, oxidation tank；
The outfan of described filtrate box is connected with the input of lime white tank, acid precipitation device setting respectively by filtrate pump,
The outfan of described lime white tank is connected with desulfurization spray section setting by milk of lime pump, setting lime cream in this lime white tank
Serosity；
The outfan of described lye tank passes through lye pump and the setting that is connected in waste water tank, and the outfan of this lye tank is also by alkali
Liquid pump, 3# circulating pump, 4# circulating pump are connected setting with acidifying spray section；
The discharge duct of described waste water tank and the discharge duct of oxidation tank are all connected with smoke inlet setting.
2. the calcium method catalytic cracking flue gas desulfurization dust-removal system according to claim 1 it is characterised in that：Described acidifying removes
Dirt section is pneumatic dust collection section, and described desulfurization section is Pneumatic desulphurization section；Or, the bottom vertical height of described acid precipitation device is higher than
The top vertical height of acidifying storage slurry section；Or, the input of described desulfurization depositor is disposed in proximity to the bottom of desulfurization depositor
At portion；Or, described alkali liquor is NaOH solution.
3. calcium method catalytic cracking flue gas desulfurization dust-removal system according to claim 1 it is characterised in that：Described acidifying dedusting
The pH value of the souring soln in section maintains between 3.0～5.0；Or, the bottom vertical height of described desulfurization storage slurry section is higher than
The top vertical height of the input of oxidation tank.
4. calcium method catalytic cracking flue gas desulfurization dust-removal system according to claim 1 it is characterised in that：In described oxidation tank
The pH value of serosity control between 5.0～6.0；Or, the pH value of the desulfurization slurry in described desulfurization section maintains 5.0～
7.0 between；Or, described lime milk liquid energy enough makes the pH value of serosity in desulfurization section maintain between 5.0～7.0.
5. calcium method catalytic cracking flue gas desulfurization dust-removal system according to claim 1 it is characterised in that：Described solid Gypsum Fibrosum
Forming step be：When in oxidation tank concentration of slurry be higher than 15%～18%, pH value between 5.0～6.0 when, oxidation tank entoplasm
Calcium sulfite in liquid generates larger gypsum crystal through oxidizing and crystallizing, then carries out thickening generation high-purity low-water-content
Solid Gypsum Fibrosum.
6. the calcium method catalytic cracking flue gas desulfurization dust-removal system according to any one of claim 1 to 5 it is characterised in that：Institute
State desulfurization spray section and include spaced upper desulfurization spray section and lower desulfurization spray section, the Pneumatic desulfuration unit of described desulfurization section
It is arranged between desulfurization spray section and lower desulfurization spray section, described system also includes 1# circulating pump and 2# circulating pump, described 1#
The input of circulating pump and desulfurization are store slurry section and are connected setting, and the outfan of this 1# circulating pump is connected with upper desulfurization spray section and sets
Put, the outfan that the input of this 1# circulating pump also returns pump with milk of lime pump, desulfurization section respectively is connected setting, described 2# follows
The input of ring pump and desulfurization are store slurry section and are connected setting, and the outfan of this 2# circulating pump is connected with lower desulfurization spray section and sets
Put.
7. the calcium method catalytic cracking flue gas desulfurization dust-removal system according to any one of claim 1 to 5 it is characterised in that：Institute
State acidifying spray section and include spaced upper acidifying spray section and lower acidifying spray section, the Pneumatic desulphurization of described acidifying dedusting section
Dust removing units are arranged between acidifying spray section and lower acidifying spray section, and described system also includes 3# circulating pump and 4# circulation
Pump, the input of described 3# circulating pump is connected setting with acidifying storage slurry section, and the outfan of this 3# circulating pump is sprayed with upper acidifying
Section is connected setting, and the input of this 3# circulating pump is also connected with the outfan of lye pump setting, described 4# circulating pump defeated
Enter end to be connected setting with acidifying storage slurry section, the outfan of this 4# circulating pump is connected setting with the lower spray section that is acidified, and this 4# follows
The input of ring pump is also connected with the outfan of lye pump setting.
8. the calcium method catalytic cracking flue gas desulfurization dust-removal system according to any one of claim 1 to 5 it is characterised in that：Institute
System of stating also includes post processing zone melt pit and sump pump, is provided with melt pit serosity, described post processing zone ground in this post processing zone melt pit
The outfan in hole passes through sump pump and the setting that is connected in oxidation tank.
9. the calcium method catalytic cracking flue gas desulfurization dust-removal system according to any one of claim 1 to 5 it is characterised in that：Institute
State oxidation tank to be also connected with roots blower setting, the outfan of roots blower and the aerating pipelines being arranged at oxidation tank inner bottom part
Be connected setting；Described waste water tank is also connected with compressed air cylinder setting, the outfan of compressed air cylinder be arranged at waste water
The aerating pipelines of case inner bottom part are connected setting.
10. the calcium method catalytic cracking flue gas desulfurization dust-removal system as described in any one of claim 1 to 9 is in flue gas desulfurization and dedusting side
Application in face.
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