CN110182838A - A kind of modified technique system and method for flue gas desulfurization ash - Google Patents
A kind of modified technique system and method for flue gas desulfurization ash Download PDFInfo
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- CN110182838A CN110182838A CN201910555301.3A CN201910555301A CN110182838A CN 110182838 A CN110182838 A CN 110182838A CN 201910555301 A CN201910555301 A CN 201910555301A CN 110182838 A CN110182838 A CN 110182838A
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- slurries
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- flue gas
- gas desulfurization
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
- C01F11/464—Sulfates of Ca from gases containing sulfur oxides
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B11/00—Calcium sulfate cements
- C04B11/02—Methods and apparatus for dehydrating gypsum
- C04B11/028—Devices therefor characterised by the type of calcining devices used therefor or by the type of hemihydrate obtained
- C04B11/032—Devices therefor characterised by the type of calcining devices used therefor or by the type of hemihydrate obtained for the wet process, e.g. dehydrating in solution or under saturated vapour conditions, i.e. to obtain alpha-hemihydrate
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B11/00—Calcium sulfate cements
- C04B11/02—Methods and apparatus for dehydrating gypsum
- C04B11/028—Devices therefor characterised by the type of calcining devices used therefor or by the type of hemihydrate obtained
- C04B11/036—Devices therefor characterised by the type of calcining devices used therefor or by the type of hemihydrate obtained for the dry process, e.g. dehydrating in a fluidised bed or in a rotary kiln, i.e. to obtain beta-hemihydrate
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B11/00—Calcium sulfate cements
- C04B11/26—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke
- C04B11/262—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke waste gypsum other than phosphogypsum
- C04B11/264—Gypsum from the desulfurisation of flue gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/91—Use of waste materials as fillers for mortars or concrete
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
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- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of modified technique system and methods of flue gas desulfurization ash.Modified technique system of the present invention includes ash cellar, acid tank, slurry tank, slurries pump, forces flow state reactivity device, slurry pool, solid-liquid separator, dehydration reactor, blower one, blower two.The method of the present invention is mainly on the basis of conventional aeration oxidation technology, the comprehensive gentle membranous wall of hard shell for abolishing desulfurization gray surface package using multiple enhancements is built, promote calcium sulfite and lime in Desulphurization all to expose and disperses, ensure to realize Efficient Conversion and stabilisation, while removing blending and covering property impurity to effectively improve product grade.It is different from conventional oxidation or method of modifying, Desulphurization is through the modified a variety of phase gypsum products for directly obtaining high-purity of system and method for the invention, it can be respectively used to downstream medium and high quality building material, self-leveling material, cementitious material and mould product etc., it is ensured that can be all by resource utilization.
Description
Technical field
The invention belongs to environmental protections and inorganic mineral material preparation technical field, and in particular to it is a kind of by calcium backbone method or
The modified flue gas desulfurization for being converted to a variety of high purity gypsum powder products, realizing resource utilization of semi-dry process flue gas desulphurization by-product
The modified technique system and method for ash.
Background technique
Sulfur dioxide in coal fired thermal power plant, steel, smelting and the flue gas of Industrial Stoves discharge is to cause acid rain, sulfuric acid cigarette
The important component of mist and Brownish haze pollution, effective method of controlling is to implement in full flue gas desulfurization.In numerous flue gas desulfurization
In technique, semidry method or dry flue gas desulphurization technique are with process is short, equipment is few, occupied area is small and excellent without technique waste water etc.
Point is particularly suitable for applying in the flue-gas desulfurizing engineering of water-deficient area.Wherein, it as the calcium base semidry method of absorbent or is done using lime
Method flue gas desulfurization technique occupies biggish market ratio because cost is relatively low.But the economical rationality of desulfurizing byproduct disposition becomes
The a great problem that this kind of technique promotes and applies.
Calcium backbone method or the main component of semi-dry desulphurization ash are calcium sulfite, and contain the complete CaO of part unreacted
Or Ca (OH)2, in addition there are the impurity such as calcium carbonate and flying dust.The partial size very little of Desulphurization, it is many de- generally mostly at 3~20 μm
The Desulphurization of sulphur engineering output is based on the particle of 10 μm or less sizes.Have more experimental study and shows homogeneous sulphite
Oxidation be easier to realize, but the Desulphurization of dry state deals with and wants much more difficult.Directly generally required with air dry oxidation
Temperature is controlled at 400~700 DEG C, time-consuming 4~6h oxygenation efficiency can be only achieved 80% or more, and product is impure more nothing
H 2 O calcium sulphate.Gas-liquid-solid three-phase wet oxidation is generally also required to be aerated for a long time, Desulphurization could be converted to calcium sulphate dihydrate
Based on product, excess aeration energy consumption is quite big.There is research to attempt using strong oxidizers assisted oxidations such as hydrogen peroxide, ozone, or
Person promotes oxidation process using additional catalyst, but cost is excessively high, using being restricted.Therefore, the modified work of conventional desulfurization ash
Process is all that Desulphurization is converted to impurity more dihydrate gypsum or anhydrous gypsum, although being able to solve stability substantially
Problem, but higher cost need to be paid, and only obtain low value mix products, it is big, economical that Desulphurization comprehensively utilizes difficulty
It is ineffective.
Studies have shown that calcium-based desulfurization ash is the SO in pulverized limestone and flue gas2Undergo gas-liquid-solid phase reaction (semidry method) or
Gas-particle two-phase reacts the product of (dry method): in a very short period of time, the SO in flue gas2It is brilliant that calcium sulfite is generated with lime reaction
Body, while absorbent granules surface moisture evaporates quickly, forms fine and close product layer and is wrapped in fresh lime powder particle surface.It is this
Product layer shell prevents further gas-solid desulphurization reaction, so that internal new fresh lime fails to expose and participate in react to be disappeared
Consumption, thus residual quantity is larger.Meanwhile the superfine small Desulphurization of partial size is also mingled with other components of coal ash, and irregular shape is presented
Looks and microstructure.Find that the fine grained outer surface of this dry state is also coated by one layer of air film, due to gas by further investigation
Film has very strong compactness, and desulfurization ash particle is difficult to soak when with slurry, and dissolution reaction resistance increases, and reaction rate is limited
System.So only being difficult to obtain efficient oxidation effectiveness by conventional aeration, impurity can not be effectively removed, improve product purity.
We wrap up in air film and hard product shell double combination obstacle is started with from effectively abolishing outside particle, will using a variety of cooperative reinforcing measures
Desulphurization highly effective reaction is stabilized simultaneously, removes the various impurity of product to improve purity, and further integrates dehydration and be modified
Unit, to obtain a variety of gypsum products for having higher-value on a production line.
Summary of the invention
The first purpose of this invention be for energy consumption existing for conventional desulfurization ash modified technique method and it is at high cost and
The problem of more added values of impurity in products are low, difficult utilization, provides a kind of modified technique system of flue gas desulfurization ash.
The first purpose of this invention is realized by the following technical solutions: the modified technique of flue gas desulfurization ash
System, it includes ash cellar, acid tank, slurry tank, slurries pump, forces flow state reactivity device, slurry pool, solid-liquid separator, dehydration
Device, blower one, blower two；The outlet of ash cellar and acid tank is connected to by pipeline with slurry tank, and blender is equipped in slurry tank；It forces
Flow state reactivity device is located at the top of slurry pool, forces flow state reactivity device outlet at bottom by pipeline or is directly connected to slurry pool；
The slurry tank outlet and slurries bottom of pond portion bypass outlet are pumped by slurries and the liquid phase of pipeline and the pressure flow state reactivity device
Entrance connection；The bottom of slurry pool and slurry tank is connect with blower one by pipeline be passed through air aeration respectively；Slurry pool
Outlet and the import of solid-liquid separator pass through piping connection, and the solid outlet of solid-liquid separator passes through conveyer belt or auger conveyor
It is connected with the material inlet of dehydration reactor, the liquid-phase outlet of solid-liquid separator is connected to by pipeline with the slurry tank, Gu
The top of liquid/gas separator is equipped with wash water entrance；The top of the dehydration reactor is equipped with exhaust outlet, exhaust outlet by blower two and
Pipeline is connected to the air inlet for forcing flow state reactivity device, and dehydration reactor is connected with the pipeline for being passed through air or water vapour,
Dehydration reactor bottom is equipped with solid matter outlet；Each pipeline is equipped with valve.
Specifically, the dehydration reactor uses the reactor with heating and temperature incubation function, quantity is 1~24, when
When quantity is 2 or more, arranged using serial or parallel connection mode.
Specifically, the pressure flow state reactivity device includes necking segment i.e. venturi section and packing section, it which is provided with liquid phase and enter
Mouthful and air inlet, several moveable spherical, spheroid shapes or cylindrical filler are built-in in packing section.
Specifically, the solid-liquid separator is using in vacuum band-type filter machine, vacuum drum or centrifugal separation equipment
It is a kind of.
Second object of the present invention is to provide the flue gas desulfurization of the modified technique system based on above-mentioned flue gas desulfurization ash
The modified technique method of ash, it includes the following steps:
(1) by ash cellar flue gas desulfurization ash and solid-liquid separator liquid-phase outlet recycle-water in slurry tank mixing preparation
The slurries for being 12~50% at solid content, then with the pH value of sulfuric acid or hydrochloric acid adjusting slurries in acid tank to 3.5~7.5；
(2) 10~100min of air aeration is passed through into the slurries of slurry tank and slurry pool by blower one, passes through slurries
Pump squeezes into the slurries in slurry tank and forces flow state reactivity device, and the air-flow for sending slurries with blower two comes into full contact with, and then one
And enter slurry pool；
(3) it pumps to squeeze into the fraction slurries reflux in slurry pool by slurries and forces flow state reactivity device, and will be in slurry pool
The dross of slurry surface is removed, and the slurries in slurry pool are then transferred to solid-liquid separator filtering and are washed simultaneously；
(4) filtrate in solid-liquid separator and wash water pass through its liquid-phase outlet and pipeline returns to slurry tank for deploying slurries
With the solid isolated then is transferred in dehydration reactor；
(5) it is passed through air or water vapour into dehydration reactor and controls temperature and is carried out dehydrating at 60~300 DEG C, controls
Solid material processed stops 2min~300min in dehydration reactor, is vented by blower two；
(6) after dehydration reactor cooling, solid material therein is drawn off to get steady to quality by its solid matter outlet
Fixed high purity gypsum powder.
Specifically, the slurry tank and slurry pool aeration process, total aeration intensity is 1~30L/m2S controls gas
The diameter of bubble is 0.1 μm~10mm.
Specifically, by forcing the gas velocity control of flow state reactivity device necking segment to control in 30~120m/s, liquid-gas ratio 10
~300L/m3In the range of.Under the various effects such as the impact, shearing, suddenly changing pressure intensity of high-speed flow, desulfurization gray surface air film and
Desulfurization product shell is destroyed, and the materials inside exposed is wetted, along with the suspension flow of built-in filler and desulfurization ash particle
State is formed by strong turbulence, phase mutual friction and collision, so that Desulphurization causes gas-liquid-solid three by further grinding distribution
Phase close contact, to efficiently carry out mass transfer and heat transfer.
Specifically, specific control method and condition are as follows when dehydration reactor operation:
When to produce the gypsum product of two water phases: being passed through air and control reactor temperature in 60~120 DEG C, solid phase
Residence time of material is in 2min~60min range；When to produce the i.e. building gypsum product of β-gypsum containing half of crystallization water: logical
Enter air and controls reactor temperature in 121~250 DEG C, solid-phase material residence time in 5min~120min range；When wanting
Produce α-gypsum i.e. high strength gypsum product when: chemical additives commonly used in the art are added into solid-phase material, and are passed through saturation
Water vapour generates saturated vapor from the moisture brought by heated material, at the same control reactor temperature 124~
250 DEG C, the solid-phase material residence time is in 20min~300min range；When anhydrous gypsum product to be produced: being passed through air and control
Temperature processed is in 251~400 DEG C, solid-phase material residence time in 30min~150min range.
Desulphurization modified technique method of the invention is comprehensive to be arranged using multiple reinforcing on the basis of conventional aeration oxidation technology
The gentle membranous wall base of hard shell for abolishing desulfurization gray surface package is applied, calcium sulfite and lime all exposures in Desulphurization are promoted
And disperse, it is ensured that realize Efficient Conversion and stabilisation, while removing blending and covering property impurity to effectively improve product grade.
It is different from conventional oxidation or method of modifying, Desulphurization is through the modified high-purity that directly obtains of system and method for the invention
A variety of phase gypsum products can be respectively used to downstream medium and high quality building material, self-leveling material, cementitious material and mould product
Deng, it is ensured that it can be all by resource utilization.In addition, present invention process system can also be used for wet desulfurization system calcium base by-product
The modification of (e.g., impure more desulfurization slag).Entire modified technique compact efficient, regulation is flexible, energy conservation and environmental protection, market
Demand adaptability is very strong.
Protrusion effect performance of the invention is as follows:
(1) Desulphurization modified technique facility compact is efficient, process water whole circulating and recovering, modifying process energy conservation and environmental protection.
(2) integrate and mix entirely using gas-liquid-solid three-phase aeration, high-intensitive strength shearing broken shell, multimedium fluidization grinding point
Dissipate and the multiple enhancements such as wet type thermal oxide ensure that Desulphurization is sufficiently converted into stable product, at the same effectively remove include it is miscellaneous
Matter effectively improves mineral grade, gypsum raw material of the Desulphurization through the modified available high-purity of the method for the present invention.
(3) two water of output, Ban Shui can be flexibly controlled on a modified technique production line and without the gypsum powder body of water phase, i.e.,
Realize the gypsum product all standing of a variety of phases, therefore, product attribute and added value are capable of the variation of the flexible adaptation market demand,
Ensure that Desulphurization or desulfurization slag can be all by resource utilizations.
Detailed description of the invention
Fig. 1 is the flowage structure schematic diagram of the modified technique system of flue gas desulfurization ash of the present invention.
Fig. 2 is the structural schematic diagram that flow state reactivity device is forced in Fig. 1.
Specific embodiment
The invention will be further described with reference to the accompanying drawings and examples.
Embodiment 1:
Referring to Fig. 1, the modified technique system of the flue gas desulfurization ash of the present embodiment, including ash cellar 1, acid tank 2, slurry tank 3, slurry
Liquid pump 4 forces flow state reactivity device 5, slurry pool 6, solid-liquid separator 7, dehydration reactor 8, blower 1, blower 2 10.From Fig. 1
In as it can be seen that the outlet of ash cellar 1 and acid tank 2 be connected to by pipeline with slurry tank 3, slurry tank 3 is interior equipped with blender 11；Wherein, grey
Desulphurization is transported to slurry tank 3 by pipeline by storehouse 1, and acid tank 2 is connected with slurry tank 3 by liquid line and passes through metering pump
Acid solution is quantitatively adding slurry tank 3 by (being not drawn into figure).Force flow state reactivity device 5 be located on slurry pool 6, and with slurry pool 6
It is connected；Slurries pump 4 passes through liquid phase entrance and slurries of the pipeline respectively with the outlet of slurry tank 3, pressure flow state reactivity device 5
The bypass outlet in pond 6 is connected.The outlet of blower 1 passes through the gas distribution pipe and aeration of pipeline and 6 bottom of slurry tank 3 and slurry pool
Element (being not drawn into figure) is connected.The outlet of slurry pool 6 and the import of solid-liquid separator 7 are separated by solid-liquid separation by piping connection
The solid outlet of device 7 is connected by conveyer belt or auger conveyor with the material inlet of dehydration reactor 8, solid-liquid separator 7
Liquid-phase outlet be connected to slurry tank 3 by pipeline, the liquid phase for isolating solid-liquid separator 7 by pipeline sends slurry back to after collecting
Liquid bath 3；The top of solid-liquid separator is equipped with wash water entrance.The top of dehydration reactor 8 is equipped with exhaust outlet, and exhaust outlet passes through blower
2 10 and pipeline with force flow state reactivity device 5 air inlet be connected to, dehydration reactor 8 is connected with the pipe for being passed through air or vapor
Road, 8 bottom of dehydration reactor are equipped with solid matter outlet.Each pipeline in above system is equipped with valve (being not drawn into figure),
For controlling the opening and closing of each pipeline.Referring to fig. 2, force have a necking segment 501 on the gas passage of flow state reactivity device 5
It is connected in series with a packing section 502,15~40 moveable plastics ball fillers is disposed in packing section 502, force stream
State reactor 5 is equipped with liquid phase entrance 503 and air inlet 504.It is in parallel and have temperature adjustment function configured with 2 in the present embodiment
The dehydration reactor 8 of energy passes through alternate operation and realizes semi continuous production.
The flue gas desulfurization ash modified technique system, to improve its degree of automation, the settable measurement in periphery and monitoring system
System, including slurry pH value and temperature, gas and slurry flow, the monitoring of dehydration reactor temperature and pressure and display instrument, with
And corresponding feedback control component；Wherein, slurry tank 3 and slurry pool 6 can be equipped with pH value and monitoring temperature instrument and respective feedback
Control mechanism, gas piping is equipped with gas velocity tolerance monitoring device and accordingly controls executing agency, and dehydration reactor can be furnished with temperature
With pressure monitor instrument and corresponding control executing agency etc..Because the equipment component and technology are existing mature technology, according to this skill
The technique requirement of art scheme, this field or those skilled in the relevant arts can design and implementation, this will not be detailed here.
Here is that the engineering of the flue gas desulfurization ash modified technique method based on above-mentioned flue gas desulfurization ash modified technique system is real
Example.
The semi-dry desulphurization ash of certain firms output is analyzed its main component calcium sulfite content 31%, calcium sulphate content
24%, calcium hydroxide content 26%, calcium carbonate 15%, other impurities 4% or so.
Method when implementing modified to Desulphurization using above-mentioned flue gas desulfurization ash modified technique system is as follows: to slurry tank 3
What the slave solid-liquid separator 7 of 1/2 volume of middle injection returned cross drainage, and by grey (about 1/10 slurry tank of flue gas desulfurization in ash cellar 1
Volume) injection slurry tank 3, it is stirred the suspension slurry for being deployed into quality solid holdup 30% or so, then by the sulfuric acid in acid tank 2
Solution is uniformly injected into above-mentioned suspension slurry, and controls slurry pH value to 4.0~5.0.Then blower 1 is opened, to slurry tank 3
Air is passed through in slurries, aeration intensity is in 2L/m in adjusting slurry tank2S or so simultaneously continues to be aerated 30min.Open slurries pump 4
Slurries in slurry tank 3 are squeezed into and force flow state reactivity device 5, while opening blower 2 10, send slurries and blower 2 10
Air-flow comes into full contact with latter and enters slurry pool 6, and gas empties (slurry pool is open) from slurry pool 6.Periodically by slurry pool 6
In fraction slurries squeeze into again and force flow state reactivity device 5, while air is passed through into slurry pool 6 by blower 1, adjusts slurry
Aeration intensity is in 15L/m in liquid pool2S, aeration time 60min or so, and the dross of slurry surface in pond is disposed.Then
Slurries are delivered to (using the vacuum belt filter) filtering of solid-liquid separator 7 and while being washed.Wherein, filtrate and wash water
Slurry tank 3 is returned after collection to be then transferred in dehydration reactor 8 and be further processed for deploying slurries, the solid material isolated.
It is passed through 200 DEG C or so of air into dehydration reactor 8 to be handled, constant temperature simultaneously controls solid material in dehydration reactor 8
5~10min is stopped, then by blower 2 10 and its pipeline connecting with dehydration reactor 8 exhaust, be vented body, which introduces, to be forced
Flow state reactivity device 5.Solid material is drawn off after being cooled to 60 DEG C to get the building gypsum of 90% or more purity is arrived, can directly gone out
It is sold after selling or being further processed into the gypsum powder body product of other specifications.Two dehydration reactors 8 feed and discharge in turn, are
Fugitive dust is avoided, dust-precipitator can be matched in discharge port.
Embodiment 2:
The Desulphurization property of the present embodiment with embodiment 1, the flue gas desulfurization ash modified technique system of use with embodiment 1,
Difference is operating method and modified product property when implementing modified to Desulphurization using the system.
Method when implementing modified to Desulphurization using above-mentioned flue gas desulfurization ash modified technique system is as follows: to slurry tank 3
What the slave solid-liquid separator 7 of 1/2 volume of middle injection returned cross drainage, and by grey (about 1/10 slurry tank of flue gas desulfurization in ash cellar 1
Volume) injection slurry tank 3, it is stirred the suspension slurry for being deployed into quality solid holdup 30% or so, then by the sulfuric acid in acid tank 2
Solution is uniformly injected into above-mentioned suspension slurry, and controls slurry pH value to 4.0~5.0.Then blower 1 is opened, to slurry tank 3
Air is passed through in slurries, aeration intensity is in 5L/m in regulating tank2S or so simultaneously continues to be aerated 30min.Slurries pump is opened slurries
Slurries in slot 3, which are squeezed into, forces flow state reactivity device 5, while opening blower 2 10, and the air-flow for sending slurries with blower 2 10 fills
Tap enters slurry pool 6 together after touch, and gas is emptied from slurry pool 6.Periodically the fraction slurries in slurry pool 6 are squeezed by force again
Flow state reactivity device 5 processed, while being passed through air into slurry pool 6 by blower 1 adjusts in the pond aeration intensity in 20L/m2·
S, aeration time 60min or so, and the dross of slurry surface in pond is disposed.Then slurries are delivered to solid-liquid separator 7
(using vacuum belt filter) filtering is simultaneously washed simultaneously.Wherein, filtrate and wash water return to slurry tank 3 for allotment after collecting
Slurries are used, and the solid material isolated is mixed into the crystal control agent (sodium tartrate or malic acid) of solid gross mass 0.3% or so
After be transferred in dehydration reactor 8 and be further processed.It is passed through 180 DEG C or so of water vapour into dehydration reactor 8 to be handled, controls
Solid material processed stops 150min isothermal reaction in dehydration reactor 8, then by blower 2 10 and its with dehydration reactor 8
The pipeline of connection is vented, and be vented body, which introduces, forces flow state reactivity device 5.Solid material is drawn off after being cooled to 60 DEG C to get arriving
α-gypsum of 90% or more purity.Two 8 alternation charging reactions of dehydration reactor and discharging can be in discharge ports to avoid fugitive dust
Configure dust-precipitator.It can sell or be sold after being further processed into the high strength gypsum powder bodies of other specifications.
Embodiment 3:
The semi-dry desulphurization ash of certain firms output is analyzed its main component calcium sulfite content 26%, calcium sulphate content
28%, calcium hydroxide content 21%, calcium carbonate content 18%, other impurities 7% or so.Its modified technique system flow and composition
Substantially with embodiment 1, difference is: the bypass outlet of slurry pool 6 by a newly-increased pump and pipeline and is forced to flow in system
The liquid phase entrance 503 of state reactor 5 is connected, and the dehydration reactor in system 8 are furnished with 1.Using the system to de-
Method when sulphur ash implements modified is as follows: the drainage of crossing of the return of slave solid-liquid separator 7 of 1/2 volume is injected into slurry tank 3, and
Slurry tank 3 is injected into flue gas desulfurization grey (about 1/8 slurry tank volume) in ash cellar 1, is stirred and is deployed into quality solid holdup
35% or so suspension slurry, then the hydrochloric acid solution in acid tank 2 is uniformly injected into above-mentioned suspension slurry, and control slurry pH value extremely
5.5~6.5.Then blower 1 is opened, air is passed through into the slurries of slurry tank 3, aeration intensity is in 10L/m in regulating tank2·
S or so simultaneously continues to be aerated 20min.It opens slurries pump and the slurries in slurry tank 3 is squeezed into pressure flow state reactivity device 5, open simultaneously
Blower 2 10, makes slurries and air-flow that blower 2 10 is sent comes into full contact with latter and enters slurry pool 6, and gas is from 6 row of slurry pool
It is empty.The fraction slurries in slurry pool 6 are squeezed into again every half an hour and force flow state reactivity device 5, while passing through blower 1 to slurry
It is passed through air in liquid pool 6, adjusts in the pond aeration intensity in 12L/m2S, aeration 30min or so, and by slurry surface in pond
Dross dispose.Then slurries are delivered to (using the vacuum belt filter) filtering of solid-liquid separator 7 and while carry out water
It washes.Wherein, filtrate and wash water return to slurry tank 3 for deploying slurries after collecting, and it is anti-that the solid material isolated then is transferred to dehydration
It answers and is further processed in device 8.It is passed through 60~80 DEG C of air into dehydration reactor 8 to be carried out dehydrating, controls solid material
60min or so is stopped in dehydration reactor 8, and passes through blower 2 10 and its pipeline connecting with dehydration reactor 8 exhaust, institute
It is vented body and introduces pressure flow state reactivity device 5.Solid material is drawn off to get left to purity 95% to slightly cool down after the completion of dehydration
Right dihydrate gypsum powder, can sell as downstream plastering raw material, or be further processed into other land plaster systems
It is sold after product.
The above is only several examples in embodiment of the present invention, it can not be used to limit claim protection of the invention
Range.Those skilled in the art of the present technique, can be in operating procedure and reaction item after understanding innovation and principle of the invention
Make several modifications in terms of the combining form of part, or increase some links well known in the art, these modifications and
Modification also should be regarded as without departing from protection scope of the present invention.
Claims (8)
1. a kind of modified technique system of flue gas desulfurization ash, it is characterised in that: it include ash cellar, acid tank, slurry tank, slurries pump,
Force flow state reactivity device, slurry pool, solid-liquid separator, dehydration reactor, blower one, blower two；The outlet of ash cellar and acid tank is logical
It crosses pipeline to be connected to slurry tank, blender is equipped in slurry tank；It forces flow state reactivity device to be located at the top of slurry pool, forces fluidised form
Reactor bottom outlet is by pipeline or is directly connected to slurry pool；The slurry tank outlet and slurries bottom of pond portion bypass outlet are logical
Slurries pump and pipeline is crossed to be connected to the liquid phase entrance for forcing flow state reactivity device；The bottom of slurry pool and slurry tank passes through respectively
Pipeline connect with blower one and is passed through air aeration；The outlet of slurry pool and the import of solid-liquid separator pass through piping connection, Gu
The solid outlet of liquid/gas separator is connected by conveyer belt or auger conveyor with the material inlet of dehydration reactor, is separated by solid-liquid separation
The liquid-phase outlet of device is connected to by pipeline with the slurry tank, and the top of solid-liquid separator is equipped with wash water entrance；The dehydration is anti-
The top of device is answered to be equipped with exhaust outlet, exhaust outlet is connected to by blower two and pipeline with the air inlet for forcing flow state reactivity device,
Dehydration reactor is connected with the pipeline for being passed through air or water vapour, and dehydration reactor bottom is equipped with solid matter outlet；It is described each
Pipeline is equipped with valve.
2. the modified technique system of flue gas desulfurization ash according to claim 1, it is characterised in that: the dehydration reactor uses
Reactor with heating and temperature incubation function, quantity are 1~24, when quantity is 2 or more, using serial or parallel connection mode
Arrangement.
3. the modified technique system of flue gas desulfurization ash according to claim 1, it is characterised in that: the pressure flow state reactivity device
Including necking segment, that is, venturi section and packing section, liquid phase entrance and air inlet which is provided with, being built-in with several in packing section can
Mobile spherical shape, spheroid shape or cylindrical filler.
4. the modified technique system of flue gas desulfurization ash according to claim 1, it is characterised in that: the solid-liquid separator is adopted
With one of vacuum band-type filter machine, vacuum drum or centrifugal separation equipment.
5. a kind of modified technique side of the flue gas desulfurization ash of the modified technique system based on the ash of flue gas desulfurization described in claim 1
Method, it is characterised in that include the following steps:
(1) by ash cellar flue gas desulfurization ash and solid-liquid separator liquid-phase outlet recycle-water in slurry tank mixing preparation Cheng Gu
The slurries that content is 12~50%, then with the pH value of sulfuric acid or hydrochloric acid adjusting slurries in acid tank to 3.5~7.5；
(2) it is passed through 10~100min of air aeration by slurries of the blower one into slurry tank and slurry pool, pumps handle by slurries
Slurries in slurry tank, which are squeezed into, forces flow state reactivity device, and the air-flow for sending slurries with blower two comes into full contact with, then one goes forward side by side
Enter slurry pool；
(3) it pumps to squeeze into the fraction slurries reflux in slurry pool by slurries and forces flow state reactivity device, and by slurries in slurry pool
The dross on surface is removed, and the slurries in slurry pool are then transferred to solid-liquid separator filtering and are washed simultaneously；
(4) filtrate in solid-liquid separator and wash water pass through its liquid-phase outlet and pipeline returns to slurry tank for deploying slurries, divide
The solid separated out is then transferred in dehydration reactor；
(5) it is passed through air or water vapour into dehydration reactor and controls temperature and is carried out dehydrating at 60~300 DEG C, control is solid
Body material stops 2min~300min in dehydration reactor, is vented by blower two；
(6) after dehydration reactor cooling, solid material therein is drawn off to get stable to quality by its solid matter outlet
High purity gypsum powder.
6. the modified technique method of the flue gas desulfurization ash of the modified technique system of flue gas desulfurization ash according to claim 5,
Be characterized in that: the slurry tank and slurry pool aeration process, total aeration intensity are 1~30L/m2S controls the straight of bubble
Diameter is 0.1 μm~10mm.
7. the modified technique method of the flue gas desulfurization ash of the modified technique system of flue gas desulfurization ash according to claim 5,
It is characterized by and the gas velocity control of flow state reactivity device necking segment is forced to control in 30~120m/s, liquid-gas ratio in 10~300L/
m3In the range of.
8. the modified technique method of the flue gas desulfurization ash of the modified technique system of flue gas desulfurization ash according to claim 5,
Be characterized in that: specific control method and condition are as follows when dehydration reactor operation:
When to produce the gypsum product of two water phases: being passed through air and control reactor temperature in 60~120 DEG C, solid-phase material
Residence time is in 2min~60min range；When to produce the i.e. building gypsum product of β-gypsum containing half of crystallization water: being passed through sky
Gas simultaneously controls reactor temperature in 121~250 DEG C, solid-phase material residence time in 5min~120min range；When producing
When α-gypsum, that is, high strength gypsum product: chemical additives commonly used in the art being added into solid-phase material, and are passed through saturated water steaming
Vapour generates saturated vapor from the moisture brought by heated material, while controlling reactor temperature 124~250
DEG C, the solid-phase material residence time is in 20min~300min range；When anhydrous gypsum product to be produced: being passed through air and control
Temperature is in 251~400 DEG C, solid-phase material residence time in 30min~150min range.
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