CN208414108U - A kind of incineration of refuse flyash or kiln ash water lotion evaporate salt making system - Google Patents
A kind of incineration of refuse flyash or kiln ash water lotion evaporate salt making system Download PDFInfo
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- CN208414108U CN208414108U CN201820174177.7U CN201820174177U CN208414108U CN 208414108 U CN208414108 U CN 208414108U CN 201820174177 U CN201820174177 U CN 201820174177U CN 208414108 U CN208414108 U CN 208414108U
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Abstract
A kind of incineration of refuse flyash of the utility model or kiln ash water lotion evaporation salt making system belong to high-salt wastewater process field.Its purpose is to provide the long incineration of refuse flyash of one kind easy to operate, high treating effect, service life of equipment or kiln ash water lotion evaporation salt making system.A kind of incineration of refuse flyash of the utility model or kiln ash water lotion evaporation salt making system include falling-film evaporating unit, forced circulation crystalline element and constant gradient decrease temperature crystalline unit；Independent condensation water collection system, fixed gas processing system, function of mechanical steam recompression system are equipped in each unit；It is equipped with separation equipment in forced circulation crystalline element, sylvite, sodium salt is separated, improves out salt quality；During the flying dust water lotion to high salinity evaporates salt manufacturing, equipment is not easy to form a scab incineration of refuse flyash or kiln ash water lotion the evaporation salt making system of the utility model, the good quality of output salt, system run all right.
Description
Technical field
The utility model belongs to high-salt wastewater process field, is used for incineration of refuse flyash or kiln buck more particularly to one kind
The processing unit of washing lotion.
Background technique
Domestic garbage incineration flyash refers to the fine particle swum in flue gas generated in incineration process of domestic garbage
Object is collected and is got by flue gas purification system trapping and flue and chimney bottom sedimentation.Contain dioxin, heavy metal in flying dust
Etc. poisonous and harmful substances be listed in danger wastes, need safety properly disposition, can be with using cement kiln synergic processing flying dust technique
Innoxious, disposal of resources flying dust, but complicated component, salt content high flying dust water can be generated during flying dust water-washing pre-treatment
Washing lotion, the potassium containing 6wt%-15wt% or so, sodium salt in this flying dust water lotion, and Potash Resources in China relative scarcity, if
Potassium, sodium salt can be produced by the evaporation of flying dust water lotion, China's sylvite vacancy will be alleviated.
Utility model content
The utility model is to provide a kind of easy to operate, high treating effect, equipment to solve the above technical problem
Incineration of refuse flyash or kiln ash water lotion evaporation salt making system with long service life and method.
The utility model relates to a kind of incineration of refuse flyash or kiln ash water lotion evaporation salt manufacturing system, the system comprises
Falling-film evaporating unit, forced circulation crystalline element and constant gradient decrease temperature crystalline unit；
The falling-film evaporating unit include preheater, falling film evaporator, falling film separator, pans, the first scrubber system,
First condensation water collection system, the first fixed gas processing system, the first function of mechanical steam recompression system；
The forced circulation crystalline element includes forced-circulation evaporator, forced circulation crystallizer, solid-liquid separator, slurries
Tank, stiff tank, the first centrifuge, the second scrubber system, the second condensation water collection system, the second fixed gas processing system, second
Function of mechanical steam recompression system；
The constant gradient decrease temperature crystalline unit includes: decrease temperature crystalline tank, crystallizing tank, magma tank, the second centrifuge, mother liquor
Tank, third function of mechanical steam recompression system, third condensation water collection system, third fixed gas processing system, cooler；
Charging pump discharge is communicated with preheater cold flow import, the outlet of preheater cold flow and falling film evaporator liquor inlet phase
It is logical；Falling film evaporator material liquid outlet is communicated with falling film separator liquor inlet, circulating pump liquor inlet, the falling film evaporator
Material liquid outlet is communicated with transfering material pump liquor inlet, and transfering material pump material liquid outlet is connected to each other with pans liquor inlet；Pans feed liquid
Outlet is connected to each other with elevator pump liquor inlet；Circulating pump material liquid outlet and preheater are connected to each other into falling film evaporator pipeline；Falling liquid film
Separator material liquid outlet is communicated with falling film evaporator into circulating pump pipeline, the steam (vapor) outlet of falling film separator and the first scrubber system
Steam inlet be connected to each other；The steam (vapor) outlet of first scrubber system is communicated with the first function of mechanical steam recompression System steam import；
First function of mechanical steam recompression system steam outlet is communicated with falling film evaporator steam inlet；Jet chimney and preheater are given birth into drop
Film evaporator feed liquid pipeline communicates；Falling film evaporator fixed gas outlet, the first condensation water collection system fixed gas outlet respectively with
First fixed gas processing system import communicates；First condensation water collection system condenses water inlet and falling film evaporator condensation-water drain
It communicates, the first condensation water collection system condensation-water drain flows into mouth, the first function of mechanical steam recompression system with preheater hot respectively
Spray water inlet communicates；Preheater hot outflux is communicated with the first condensation water collection system；
The forced circulation crystallizer feed solution outlet is communicated with solid-liquid separator liquor inlet；Solid-liquid separator material liquid outlet
It is communicated with forced circulation pump liquor inlet, forced circulation pump material liquid outlet is communicated with forced-circulation evaporator liquor inlet；It is promoted
Pump material liquid outlet is communicated with solid-liquid separator into forced circulation pump pipeline, forced-circulation evaporator material liquid outlet and forced circulation knot
Brilliant device liquor inlet communicates；The outlet of forced circulation crystallizer feed solution is communicated with serum pot liquor inlet；Serum pot material liquid outlet with
Slurries pump liquor inlet communicates；Slurries pump material liquid outlet is communicated with stiff tank liquor inlet；Stiff tank material liquid outlet and first from
Scheming import communicates, and the first centrifuge mother liquor outlet is communicated with pans mother liquor import；Solid-liquid separator supernatant outlet and drop
Warm crystallizing tank liquor inlet communicates；Forced circulation crystallizer steam (vapor) outlet is communicated with the second scrubber system steam inlet；Second washes
Gas system steam outlet is communicated with the second function of mechanical steam recompression System steam import；Second function of mechanical steam recompression System steam
Outlet is communicated with forced-circulation evaporator steam inlet；The outlet of forced-circulation evaporator fixed gas, the second condensation water collection system
Fixed gas outlet is communicated with the second fixed gas processing system import respectively；Second condensation water collection system import is followed with pressure respectively
Ring evaporator condensation water out communicates, the second condensation water collection system outlet with the second function of mechanical steam recompression system shower water into
Mouth communicates；
The solid-liquid separator supernatant discharge port is communicated with decrease temperature crystalline tank feed inlet；Decrease temperature crystalline tank discharge port and knot
Brilliant tank feed inlet communicates；Crystallizing tank discharge port is communicated with discharging pump feed inlet；Discharging pump discharge port is communicated with magma tank, magma tank
Discharge port is communicated with the second centrifuge liquor inlet；Second centrifuge mother liquor outlet is communicated with mother liquor tank liquor inlet, mother liquor tank
Material liquid outlet is communicated with mother liquor pump liquor inlet；Mother liquor pumps out material mouth and communicates with pans feed inlet, crystallizing tank steam (vapor) outlet with
Third function of mechanical steam recompression System steam import communicates, third function of mechanical steam recompression system steam outlet and cooler hot-fluid
Import communicates；Cooler hot outlets are communicated with third condensation water collection system import；Third condensation water collection system fixed gas
Outlet is communicated with third fixed gas processing system import.
The outlet of the first condensation water collection system flows into mouth with preheater hot and communicates in the utility model, i.e. preheater hot-fluid is adopted
It is preheated with the condensed water that falling film evaporator generates.
Raw jet chimney is communicated with preheater into falling film evaporator feed liquid pipeline in the utility model；I.e. raw steam heating is adopted
The mode heated with raw steam directly to feed liquid in feed pipe.
Preferably, the falling film separator and forced circulation crystallizer are equipped with Despumation device；The forced circulation crystallization
Device salt foot is equipped with washing device；The decrease temperature crystalline tank jacketed.
Preferably, the decrease temperature crystalline tank is carried out cold using feed liquid to be processed (i.e. incineration of refuse flyash or kiln ash water lotion)
But cool down.
Preferably, the crystallizing tank is using flash distillation cooling.
Preferably, the decrease temperature crystalline tank, crystallizing tank include turbine type agitator.
Preferably, the stiff tank includes turbine type agitator.
Preferably, the magma tank includes cyclone separator, turbine type agitator.
Preferably, the falling-film evaporating unit, forced circulation crystalline element are micro-vacuum state.
A kind of method that the utility model further relates to incineration of refuse flyash or the evaporation salt manufacturing of kiln ash water lotion, the method packet
Include following steps:
A preheating: feed liquid to be processed enters preheater and is warming up to 45 DEG C -65 DEG C, is fed the heating of liquid pipe road, material by raw steam
Liquid is warming up to 90 DEG C -100 DEG C；
B falling film evaporation: the feed liquid after preheating enters falling film evaporator, and evaporating temperature is controlled in falling film evaporator 90
℃-100℃；Falling film evaporator discharge feed liquid enter falling film separator, feed liquid is concentrated by evaporation in falling film separator, steam into
Enter scrubber system, concentrate solution is back to falling film evaporator；Reach 20%-25% to solid-to-liquid ratio in feed liquid, carries out step (c)
Operation；
C forced-circulation evaporation: enter forced-circulation evaporator by the feed liquid that step b is handled, in forced-circulation evaporator
Interior control evaporating temperature is at 100 DEG C -110 DEG C；Reach >=30% to solid-to-liquid ratio in feed liquid, carries out the operation of step (d)；
D separation, crystallization: forced circulation crystallizer and solid-liquid separator are sequentially entered by the feed liquid that step c is handled, through solid
The isolated supernatant of liquid/gas separator and magma；Forced circulation crystallizer is eluriated using chlorination mother liquid of sodium；The chlorination
The mother liquor that mother liquid of sodium comes out from the first centrifuge, it is anti-blocking that chlorination mother liquid of sodium plays the role of classification, cooling, salt foot；
E supernatant enters constant gradient decrease temperature crystalline unit, obtains crystalline potassium chloride；
F magma, which enters, to continue to evaporate in forced-circulation evaporator；
The feed liquid to be processed is incineration of refuse flyash or kiln ash water lotion.
Preferably, the preheater hot-fluid is the condensed water that falling film evaporator generates, and condensate temperature is 80 DEG C -100 DEG C.
Preferably, using feed liquid to be processed, (i.e. waste incineration flies decrease temperature crystalline tank in the constant gradient decrease temperature crystalline unit
Ash or kiln ash water lotion) it cools down, feed liquid temperature is down between 50 DEG C -70 DEG C.
Preferably, crystallizing tank is cooled down using flash evaporation technology in the constant gradient decrease temperature crystalline unit, feed liquid temperature drop
To between 40 DEG C -30 DEG C.
Preferably, the steam generated in falling film separator, forced circulation crystallizer enters after scrubber system gas washing respectively
Function of mechanical steam recompression system is overpressurized and is warming up to 90 DEG C -110 DEG C.
A kind of incineration of refuse flyash of the utility model or kiln ash water lotion evaporation salt making system and method and the prior art are not
It is with place:
The utility model incineration of refuse flyash or kiln ash water lotion evaporate salt making system to the flying dust water lotion of high salinity
During evaporating salt manufacturing, equipment is not easy to form a scab, the good quality of output salt, system run all right.
Go out the identification of salt quality after the method processing of the utility model incineration of refuse flyash or the evaporation salt manufacturing of kiln ash water lotion
Data, and finally providing corresponding testing result.
Detailed description of the invention
Fig. 1 is the structural schematic diagram that the utility model incineration of refuse flyash or kiln ash water lotion evaporate salt making system, wherein
1, preheater；2, falling film evaporator；3, falling film separator；4, pans；5, forced-circulation evaporator；6, forced circulation crystallizes
Device；7, serum pot；8, stiff tank；9, the first centrifuge；10, solid-liquid separator；11, decrease temperature crystalline tank；12, crystallizing tank；13, brilliant
Starch tank；14, the second centrifuge；15, the first condensation water collection system；16, the first scrubber system；17, the first mechanical vapour is pressed again
Compression system；18, the second condensation water collection system；19, the second scrubber system；20, the second function of mechanical steam recompression system；21,
Three function of mechanical steam recompression systems；22, third condensation water collection system；23, mother liquor tank；24, the first fixed gas processing system；
25, cooler；26, the second fixed gas processing system；27, third fixed gas processing system.
Specific embodiment
It is steamed by following embodiment and verification test a kind of incineration of refuse flyash or kiln ash water lotion to the utility model
Hair salt making system is further described.
Embodiment 1
Incineration of refuse flyash or kiln ash water lotion the evaporation salt making system of the present embodiment include falling-film evaporating unit, force to follow
Ring crystalline element and constant gradient decrease temperature crystalline unit；
Falling-film evaporating unit includes preheater 1, falling film evaporator 2, falling film separator 3, pans 4, the first scrubber system
16, the first condensation water collection system 15, the first fixed gas processing system 24, the first function of mechanical steam recompression system 17；
Forced circulation crystalline element includes forced-circulation evaporator 5, forced circulation crystallizer 6, solid-liquid separator 10, slurries
Tank 7, stiff tank 8, the first centrifuge 9, the second scrubber system 19, the second condensation water collection system 18, the second fixed gas processing system
The 26, second function of mechanical steam recompression system 20 of system；
Constant gradient decrease temperature crystalline unit includes: decrease temperature crystalline tank 11, crystallizing tank 12, magma tank 13, the second centrifuge 14, mother
It is flow container 23, third function of mechanical steam recompression system 21, third condensation water collection system 22, third fixed gas processing system 27, cold
But device 25；
Charging pump discharge is communicated with 1 cold flow import of preheater, the outlet of 1 cold flow of preheater and 2 liquor inlet of falling film evaporator
It communicates；2 material liquid outlet of falling film evaporator is communicated with 3 liquor inlet of falling film separator, circulating pump liquor inlet, falling film evaporator 2
Material liquid outlet communicated with transfering material pump liquor inlet, transfering material pump material liquid outlet is connected to each other with 4 liquor inlet of pans；Pans 4
Material liquid outlet is connected to each other with elevator pump liquor inlet；Circulating pump material liquid outlet is communicated with preheater 1 into 2 pipeline of falling film evaporator
It connects；3 material liquid outlet of falling film separator is communicated with falling film evaporator 2 into circulating pump pipeline, the steam (vapor) outlet of falling film separator 3 and
The steam inlet of one scrubber system 16 is connected to each other；The steam (vapor) outlet of first scrubber system 16 and the first function of mechanical steam recompression system
17 steam inlets communicate；First function of mechanical steam recompression system, 17 steam (vapor) outlet is communicated with 2 steam inlet of falling film evaporator；It is raw to steam
Steam pipe road is communicated with preheater 1 into 2 feed liquid pipeline of falling film evaporator；The outlet of 2 fixed gas of falling film evaporator, the first condensation water collection
The outlet of 15 fixed gas of system is communicated with 24 import of the first fixed gas processing system respectively；First condensation water collection system, 15 condensed water
Import is communicated with 2 condensation-water drain of falling film evaporator, 15 condensation-water drain of the first condensation water collection system respectively with preheater hot
Flow into mouth, the first function of mechanical steam recompression system 17 spray water inlet communicates；Preheater hot outflux and the first condensation water collection
System 15 communicates；
6 material liquid outlet of forced circulation crystallizer is communicated with 10 liquor inlet of solid-liquid separator；10 feed liquid of solid-liquid separator goes out
Mouth is communicated with forced circulation pump liquor inlet, and forced circulation pump material liquid outlet is communicated with 5 liquor inlet of forced-circulation evaporator；It mentions
It rises pump material liquid outlet to communicate with solid-liquid separator 10 into forced circulation pump pipeline, 5 material liquid outlet of forced-circulation evaporator and pressure
6 liquor inlet of circulation crystallization device communicates；6 material liquid outlet of forced circulation crystallizer is communicated with 7 liquor inlet of serum pot；Serum pot 7
Material liquid outlet is communicated with slurries pump liquor inlet；Slurries pump material liquid outlet is communicated with 8 liquor inlet of stiff tank；8 feed liquid of stiff tank
Outlet is communicated with 9 import of the first centrifuge, and 9 mother liquor outlet of the first centrifuge is communicated with 4 mother liquor import of pans；Solid-liquid separator
10 supernatant outlets are communicated with 11 liquor inlet of decrease temperature crystalline tank；6 steam (vapor) outlet of forced circulation crystallizer and the second scrubber system
19 steam inlets communicate；Second scrubber system, 19 steam (vapor) outlet is communicated with 20 steam inlet of the second function of mechanical steam recompression system；
Second function of mechanical steam recompression system, 20 steam (vapor) outlet is communicated with 5 steam inlet of forced-circulation evaporator；Forced-circulation evaporator 5
Fixed gas outlet, the outlet of 18 fixed gas of the second condensation water collection system are communicated with 26 import of the second fixed gas processing system respectively；
Second condensation water collection system, 18 import is communicated with 5 condensation-water drain of forced-circulation evaporator respectively, the second condensation water collection system
22 outlet of system is communicated with the second function of mechanical steam recompression system 20 spray water inlet；
10 supernatant discharge port of solid-liquid separator is communicated with 11 feed inlet of decrease temperature crystalline tank；11 discharge port of decrease temperature crystalline tank with
12 feed inlet of crystallizing tank communicates；12 discharge port of crystallizing tank is communicated with discharging pump feed inlet；Discharging pump discharge port and 13 phase of magma tank
Logical, 13 discharge port of magma tank is communicated with 14 liquor inlet of the second centrifuge；Second centrifuge, 14 mother liquor outlet and 23 material of mother liquor tank
Liquid import communicates, and 23 material liquid outlet of mother liquor tank is communicated with mother liquor pump liquor inlet；Mother liquor pumps out material mouth and 4 feed inlet of pans
It communicates, 12 steam (vapor) outlet of crystallizing tank is communicated with 21 steam inlet of third function of mechanical steam recompression system, and third mechanical vapour is pressed again
21 steam (vapor) outlet of compression system is communicated with 25 hot-fluid import of cooler；25 hot outlets of cooler and third condensation water collection system 22
Import communicates；The outlet of 22 fixed gas of third condensation water collection system is communicated with 27 import of third fixed gas processing system.
Wherein, falling film separator 3 is equipped with Despumation device, and forced circulation crystallizer 6 is equipped with Despumation device；Forced circulation crystallization
6 salt foot of device is equipped with washing device；11 jacketed of decrease temperature crystalline tank；Decrease temperature crystalline tank 11 is cooled down using material liquid；Knot
Brilliant tank 12 is using flash distillation cooling；Decrease temperature crystalline tank 11, crystallizing tank 12 include turbine type agitator；Stiff tank 8, magma tank 13 include
Cyclone separator, turbine type agitator；Falling-film evaporating unit, forced circulation crystalline element are micro-vacuum state.
Working principle, that is, the utility model of the utility model incineration of refuse flyash or kiln ash water lotion evaporation salt making system
Incineration of refuse flyash or kiln ash water lotion evaporation salt manufacturing method: after water treatment flying dust washing feed liquid pass through feed pump
The flying dust water lotion of salt content 6wt%-15wt% by purification of water quality is lifted into preheater 1, through 80 DEG C -100 of temperature
DEG C falling film evaporator 2 generate condensed water exchange heat, so that temperature of charge is risen to 45 DEG C -65 DEG C.
Material after preheating enters falling film evaporator 2 by feed pipe, and raw steam is passed through in feed pipe directly in pipe
Material is preheated, and material is made to be warming up to 90 DEG C -100 DEG C.
Material after preheating enters the evaporation and concentration of falling film evaporator 2, and temperature control is at 90 DEG C -100 in falling film evaporator 2
DEG C, solid-to-liquid ratio of the feed liquid in falling film evaporator 2 is 20%-25% or so.
Feed liquid after the evaporation and concentration of falling film evaporator 2 enters falling film separator 3, carries out gas-liquid separation, steam is by drop
Despumation device in membrane separator 3 carries out gas washing into scrubber system, and the steam after gas washing enters function of mechanical steam recompression system
System makes gas temperature rise to 90 DEG C -110 DEG C by compressing workmanship, and liquid enters falling film evaporator 2 by circulating pump.After concentration
Feed liquid pans 4 are entered by transfering material pump
Concentrate solution in pans 4 enters forced-circulation evaporator 5 by elevator pump and is evaporated crystallization, in forced circulation
Temperature control is at 100 DEG C -110 DEG C in evaporator 5.
Feed liquid enters forced circulation crystallizer realization vapor-liquid separation after forced-circulation evaporator is concentrated, by solid-liquid point
Heavy magma carries out circulating and evaporating by forced circulation pump when from device, and the small supernatant of specific gravity enters decrease temperature crystalline tank
11.When feed liquid starts to occur crystalline solid content >=30% in forced circulation crystalline element, spinning liquid is passed through by discharging pump discharging
Separator enters stiff tank 8, goes out from stiff tank 8 and enters centrifuge, and the feed liquid containing crystal obtains moisture content after centrifugation
Salt crystallization and mother liquor, mother liquor reflux no more than 5wt% are pumped back to forced-circulation evaporator to pans 4, then by being promoted,
Realize that mother liquor recycles in system.
The supernatant isolated from solid-liquid separator 10 enters decrease temperature crystalline tank 11 by cyclone hydraulic separators and exchanges heat, and drops
Warm 11 jacketed of crystallizing tank, using feed liquid to be processed (i.e. incineration of refuse flyash or kiln ash water lotion) for the heat exchange that cools down, heat exchange
Feed liquid to be processed afterwards returns in head tank.
Discharging enters crystallizing tank 12 after cooling, manufactures vacuum environment by function of mechanical steam recompression system, carries out flash distillation reduction
Feed liquid temperature, last feed liquid enter centrifuge, and the feed liquid containing crystal obtains moisture content no more than 5wt%'s after centrifugation
Sylvite crystallization and mother liquor, mother liquor reflux to mother liquor tank 23 are returning to pans 4 by mother liquor pump circulation, realize that mother liquor is being
Circulation in system.
Salt concentration is 6wt%-15wt% in garbage flying ash water lotion, and wherein predominant amount is NaCl and KCl, through this rubbish
Rubbish flying ash or kiln ash water lotion evaporation salt making system processing unit and processing method, can output meet National Industrial solarization
The sodium chloride salt of salt secondary standard, and meet the potassium chloride salt of National Industrial salt secondary standard.
Embodiment 2
The method of incineration of refuse flyash or kiln ash water lotion the evaporation salt manufacturing of the present embodiment sequentially includes the following steps:
The incineration of refuse flyash or kiln ash water lotion of a salt concentration 10wt% enters preheater 1 by feed pump, through falling liquid film
Enter falling film evaporator after the preheating of evaporator steam condensate (SC).
B is through falling film evaporator concentration material, and after so that material solid-to-liquid ratio is reached 22%, it is single that material enters forced circulation crystallization
Member makes material solid-to-liquid ratio reach 32% through forced circulation crystalline element concentration material, makes by solid-liquid separator 10 containing on sylvite
Clear liquid enters constant gradient decrease temperature crystalline unit, and the magma of sodium salt, which enters, enters centrifuge after stiff tank 8 is thickened, and obtains
Sodium salt moisture content is 5wt%, the sodium chloride salt of sodium chloride-containing 92.5wt%.
Supernatant of the c containing sylvite enters decrease temperature crystalline tank 11, passes through feed liquid to be processed (i.e. incineration of refuse flyash or kiln buck
Washing lotion) cooling down makes its temperature reach 60 DEG C, and feed liquid enters crystallizing tank after cooling, and crystallizing tank uses flash evaporation technology, in -0.3MPa
Subnormal ambient under, feed liquid is evaporated rapidly, and feed liquid temperature is down to 40 DEG C or so.Feed liquid after cooling enters magma tank 13 and is increased
Enter centrifuge after thick, obtaining sylvite moisture content is 5wt%, the potassium chloride salt of chloride containing potassium 89wt%.
Embodiment 3
The method of incineration of refuse flyash or kiln ash water lotion evaporation salt manufacturing and the difference of embodiment 2 of the present embodiment exist
In:
The incineration of refuse flyash or kiln ash water lotion of a salt concentration 15wt% enters preheater by feed pump, through falling liquid film
Enter falling film evaporator after the preheating of evaporator steam condensate (SC)；
B material solid-to-liquid ratio in falling film evaporator reaches 20%；
C material solid-to-liquid ratio in forced-circulation evaporator reaches 35%；
D crystallizing tank feed liquid temperature is down to 35 DEG C or so；
The sodium chloride moisture content that the present embodiment obtains is 5wt%, sodium chloride-containing 94wt%；Potassium chloride moisture content is 5wt%,
Sodium chloride-containing 88wt%.
Although the foregoing describe specific embodiment of the present utility model, it will be appreciated by those of skill in the art that
These are merely examples, and the protection scope of the utility model is defined by the appended claims.Those skilled in the art
Member can make numerous variations or be repaired to these embodiments under the premise of without departing substantially from the principles of the present invention and essence
Change, but these change and modification each fall within the protection scope of the utility model.
Claims (7)
1. a kind of incineration of refuse flyash or kiln ash water lotion evaporate salt making system, it is characterised in that: the system comprises falling liquid film steamings
Bill member, forced circulation crystalline element and constant gradient decrease temperature crystalline unit；
The falling-film evaporating unit includes preheater (1), falling film evaporator (2), falling film separator (3), pans (4), first
Scrubber system (16), the first condensation water collection system (15), the first fixed gas processing system (24), the first function of mechanical steam recompression
System (17)；
The forced circulation crystalline element includes forced-circulation evaporator (5), forced circulation crystallizer (6), solid-liquid separator
(10), serum pot (7), stiff tank (8), the first centrifuge (9), the second scrubber system (19), the second condensation water collection system
(18), the second fixed gas processing system (26), the second function of mechanical steam recompression system (20)；
The constant gradient decrease temperature crystalline unit includes: decrease temperature crystalline tank (11), crystallizing tank (12), magma tank (13), the second centrifugation
Machine (14), mother liquor tank (23), third function of mechanical steam recompression system (21), third condensation water collection system (22), third are not coagulated
Gas processing system (27), cooler (25)；
Charging pump discharge communicated with preheater (1) cold flow import, preheater (1) cold flow outlet and falling film evaporator (2) feed liquid into
Mouth communicates；Falling film evaporator (2) material liquid outlet is communicated with falling film separator (3) liquor inlet, circulating pump liquor inlet, the drop
The material liquid outlet of film evaporator (2) is communicated with transfering material pump liquor inlet, transfering material pump material liquid outlet and pans (4) liquor inlet phase
It connects；Pans (4) material liquid outlet is connected to each other with elevator pump liquor inlet；Circulating pump material liquid outlet and preheater are into falling film evaporation
Device (2) pipeline is connected to each other；Falling film separator (3) material liquid outlet is communicated with falling film evaporator (2) into circulating pump pipeline, falling liquid film separation
The steam (vapor) outlet of device (3) and the steam inlet of the first scrubber system (16) are connected to each other；The steam (vapor) outlet of first scrubber system (16)
It is communicated with first function of mechanical steam recompression system (17) steam inlet；First function of mechanical steam recompression system (17) steam (vapor) outlet with
Falling film evaporator (2) steam inlet communicates；Raw jet chimney is communicated with preheater (1) into falling film evaporator (2) feed liquid pipeline；Drop
Film evaporator (2) fixed gas outlet, the first condensation water collection system (15) fixed gas outlet respectively with the first fixed gas processing system
System (24) import communicates；First condensation water collection system (15) condensation water inlet is communicated with falling film evaporator (2) condensation-water drain,
First condensation water collection system (15) condensation-water drain respectively with preheater (1) hot-fluid import, the first function of mechanical steam recompression system
System (17) spray water inlet communicates；Preheater (1) hot outlets are communicated with the first condensation water collection system (15)；
Forced circulation crystallizer (6) material liquid outlet is communicated with solid-liquid separator (10) liquor inlet；Solid-liquid separator (10)
Material liquid outlet is communicated with forced circulation pump liquor inlet, forced circulation pump material liquid outlet and forced-circulation evaporator (5) feed liquid into
Mouth communicates；Elevator pump material liquid outlet is communicated with solid-liquid separator (10) into forced circulation pump pipeline, forced-circulation evaporator (5) material
Liquid outlet is communicated with forced circulation crystallizer (6) liquor inlet；Forced circulation crystallizer (6) material liquid outlet and serum pot (7) are expected
Liquid import communicates；Serum pot (7) material liquid outlet is communicated with slurries pump liquor inlet；Slurries pump material liquid outlet and stiff tank (8) expect
Liquid import communicates；Stiff tank (8) material liquid outlet is communicated with the first centrifuge (9) import, and the first centrifuge (9) mother liquor outlet is in
Between tank (4) mother liquor import communicate；Solid-liquid separator (10) supernatant outlet is communicated with decrease temperature crystalline tank (11) liquor inlet；It forces
Circulation crystallization device (6) steam (vapor) outlet is communicated with the second scrubber system (19) steam inlet；Second scrubber system (19) steam (vapor) outlet
It is communicated with second function of mechanical steam recompression system (20) steam inlet；Second function of mechanical steam recompression system (20) steam (vapor) outlet with
Forced-circulation evaporator (5) steam inlet communicates；The outlet of forced-circulation evaporator (5) fixed gas, the second condensation water collection system
(18) fixed gas outlet is communicated with second fixed gas processing system (26) import respectively；Second condensation water collection system (18) import
It is communicated with forced-circulation evaporator (5) condensation-water drain, the second condensation water collection system (18) outlet and the second mechanical vapour are again
Compressibility (20) spray water inlet communicates；
Solid-liquid separator (10) the supernatant discharge port is communicated with decrease temperature crystalline tank (11) feed inlet；Decrease temperature crystalline tank (11) goes out
Material mouth is communicated with crystallizing tank (12) feed inlet；Crystallizing tank (12) discharge port is communicated with discharging pump feed inlet；Discharging pump discharge port with
Magma tank (13) communicates, and magma tank (13) discharge port is communicated with the second centrifuge (14) liquor inlet；Second centrifuge (14) is female
Liquid outlet is communicated with mother liquor tank (23) liquor inlet, and mother liquor tank (23) material liquid outlet is communicated with mother liquor pump liquor inlet；Mother liquor pump
Discharge port is communicated with pans (4) feed inlet, and crystallizing tank (12) steam (vapor) outlet and third function of mechanical steam recompression system (21) are steamed
Vapor inlet communicates, and third function of mechanical steam recompression system (21) steam (vapor) outlet is communicated with cooler (25) hot-fluid import；Cooler
(25) hot outlets are communicated with third condensation water collection system (22) import；The outlet of third condensation water collection system (22) fixed gas
It is communicated with third fixed gas processing system (27) import.
2. incineration of refuse flyash according to claim 1 or kiln ash water lotion evaporate salt making system, it is characterised in that: described
Falling film separator (3) and forced circulation crystallizer (6) are equipped with Despumation device；Forced circulation crystallizer (6) the salt foot is equipped with
Washing device；Decrease temperature crystalline tank (11) jacketed.
3. incineration of refuse flyash according to claim 1 or kiln ash water lotion evaporate salt making system, it is characterised in that: described
Decrease temperature crystalline tank (11) is cooled down using feed liquid to be processed；The feed liquid to be processed is incineration of refuse flyash or kiln buck
Washing lotion.
4. incineration of refuse flyash according to claim 1 or kiln ash water lotion evaporate salt making system, it is characterised in that: described
Crystallizing tank (12) is using flash distillation cooling.
5. incineration of refuse flyash according to claim 1 or kiln ash water lotion evaporate salt making system, it is characterised in that: described
Decrease temperature crystalline tank (11), crystallizing tank (12) include turbine type agitator.
6. incineration of refuse flyash according to claim 1 or kiln ash water lotion evaporate salt making system, it is characterised in that: described
Stiff tank (8) includes turbine type agitator, and the magma tank (13) includes cyclone separator, turbine type agitator.
7. incineration of refuse flyash according to claim 1 or kiln ash water lotion evaporate salt making system, it is characterised in that: described
Falling-film evaporating unit, forced circulation crystalline element are micro-vacuum state.
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| CN201820174177.7U CN208414108U (en) | 2018-01-31 | 2018-01-31 | A kind of incineration of refuse flyash or kiln ash water lotion evaporate salt making system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108191135A (en) * | 2018-01-31 | 2018-06-22 | 北京中科国润环保科技有限公司 | A kind of incineration of refuse flyash or kiln ash water lotion evaporation salt making system and method |
| CN112520760A (en) * | 2020-11-13 | 2021-03-19 | 中国恩菲工程技术有限公司 | Sodium sulfate production system |
-
2018
- 2018-01-31 CN CN201820174177.7U patent/CN208414108U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108191135A (en) * | 2018-01-31 | 2018-06-22 | 北京中科国润环保科技有限公司 | A kind of incineration of refuse flyash or kiln ash water lotion evaporation salt making system and method |
| CN112520760A (en) * | 2020-11-13 | 2021-03-19 | 中国恩菲工程技术有限公司 | Sodium sulfate production system |
| CN112520760B (en) * | 2020-11-13 | 2022-12-23 | 中国恩菲工程技术有限公司 | Sodium sulfate production system |
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