CN206104533U - SCR dead catalyst recovery system - Google Patents
SCR dead catalyst recovery system Download PDFInfo
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Abstract
The application discloses SCR dead catalyst recovery system, its characterized in that, including crushing mixing arrangement, it later is connected with calcination device to smash mixing arrangement, calcination device is used for carrying out the calcination to the mixture, be connected with a storage device after the calcination device, be connected with a filter equipment after the storage device, a storage device is connected with the 2nd storage device, be connected with the 2nd filter equipment after the 2nd storage device, be connected with the 3rd storage device after the 2nd filter equipment, be connected with the 3rd filter equipment after the 3rd storage device. The utility model discloses, the structure is formed simply, is provided with the pipeline of retrieving many places for the water consumption is low, the auxiliary agent addition is few, the aftertreatment energy consumption is low and load for a short time.
Description
Technical field
The application belongs to waste catalyst recovery field, and in particular to a kind of SCR waste catalyst recoveries system.
Background technology
SCR (SCR) is to solve NOx pollution problems denitration skill efficiently, ripe in thermal power generation at present
Again substantial amounts of solid waste is generated after art, but SCR catalyst inactivation, to environmental conservation new challenge is proposed.SCR is catalyzed
V is usually contained in agent2O5、WO3、MoO3Deng toxic metals compounds, these solid waste are processed by way of landfill, one
Aspect can cause severe contamination to soil and water body；On the other hand, tungsten, molybdenum etc. belong to rare metal resources, in SCR dead catalyst
Tungsten oxide, oxidation molybdenum content up to more than 5%, even above common tungsten ore and molybdenum ore also result in SCR dead catalyst landfill
The huge waste of valuable resource.Therefore, either from the angle of environmental conservation, or from the efficient utilization angle of rare metal
Degree, isolates and purifies to SCR dead catalyst, recycles valuable metal therein and has important social meaning and economic effect
Benefit.
The method of SCR dead catalyst separation and recovery valuable metal compound mainly includes leaching and two steps of later separation.
There are alkalization roasting method, soda boiling solvent extraction method, acidleach reducing process etc. process stages are leached；The later separation stage have the sedimentation method, from
Sub- exchange process, extraction etc..At present the separation and recovery method of SCR dead catalyst is mainly in this two big operation various methods not
With combination.During vanadium, tungsten of the Chinese patent CN104862485A in separating-purifying SCR dead catalyst, alkalized roasting by NaOH
Vanadium tungsten solution is obtained with leaching.The solution carries tungsten and obtains ammonium paratungstate by organic extraction twice and alkali liquor back extraction, and extracts residual
Vanadium in liquid obtains vanadic anhydride by process.Chinese patent CN104611564 is using NaOH soda boilings and potassium chlorate oxidation leaching
Go out to obtain vanadium tungsten solution, then ammonium metavanadate obtained by ammonium chloride precipitation, extraction raffinate calcium chloride transformation is artificial schellite, calcium molybdate,
Wolframic acid or molybdic acid product are obtained finally by HCl process.Chinese patent CN104561554A also passes through NaCO3Alkalization roasting
Burning method Leaching Vanadium tungsten solution, adjusts the pH value of solution and is 7.5～9.5 and is heated to 75～90 DEG C of remove impurity, then controls pH for 1～3
Tungsten is carried by anion exchange resin, vanadium is then stayed in extraction raffinate, finally respectively precipitation and heavy tungsten and separated vanadium, tungsten.
Although at present the method and system of SCR dead catalyst separation and recovery valuable metal is more, universal in industrialization
There is a problem of that the area that water consumption is big, additive dosage is more, post processing high energy consumption, load weight, particularly thermoelectricity are flourishing is usual
Water resources shortage, the consumption and pollution to water resource is focused more on.Because SCR dead catalyst powder still has abundant duct
With larger specific surface area, water requirement is larger in operation is leached, and dead catalyst V2O5And WO3Or MoO3Content it is less, make
Obtain vanadium in leachate relatively low with tungsten or molybdenum concentration.Current recovery method typically directly carries out purifies and separates to the leachate, by
In liquid handling amount is big, subsequent step is more, additive dosage is big, can form related liquid waste processing or high energy consumption issues.
Utility model content
The subject matter that the application is solved is to provide a kind of SCR waste catalyst recoveries system, to solve generally existing water consumption
Amount is big, many additive dosages, the post processing high energy consumption and load technical problem such as again.
In order to solve above-mentioned technical problem, the utility model discloses a kind of SCR waste catalyst recoveries system, its feature exists
In, it is described to be pulverized and mixed device for SCR dead catalyst and roasting auxiliary agent to be crushed including device is pulverized and mixed, and mix
Close uniform, obtain compound；
Described being pulverized and mixed after device is connected with calciner, and the calciner is used to carry out roasting to compound；
The first storage device is connected with after the calciner, first storage device is used for the mixing after roasting
Material carries out deionized water dipping, and the first defecator is connected with after first storage device, and first defecator is used
Material after by dipping carries out first time filtration, and filtering residue washing recovery obtains TiO2；
First storage device is connected with the second storage device, and second storage device is used for what first time was filtered
Filtrate adds calcium chloride, carries out precipitation enrichment；The second defecator, second mistake are connected with after second storage device
Filter device is used to carry out the material after enrichment second filtration, and second resulting filter liquor enters first storing
Device, reclaims for impregnating, and filtering residue returns to the second storage device；
Second storage device is used to carry out dilute hydrochloric acid washing, second defecator pair to the second filtering residue for filtering
Material after the dilute hydrochloric acid washing carries out the 3rd filtration, the filtrate filtering residue being filtrated to get for the third time；
The 3rd storage device is connected with after second defecator, the 3rd storage device is used for third time mistake
The filtering residue that filter is obtained carries out salt acid dip dissolving and obtains lysate, and ammonia adjusts the pH value of the lysate, is precipitated；
The 3rd defecator is connected with after 3rd storage device, the 3rd defecator is used to carry out the material after precipitation
4th filtration, obtains filtrate and the filtering residue of the 4th filtration, and the filtrate that the 4th filtrate filtered obtains with third time merges recovery
Calcium chloride, the filtering residue being filtrated to get for the 4th time returns to the 3rd storage device；
3rd storage device is used for the filtering residue ammonia solvent being filtrated to get to the 4th time, and filtering residue is partly dissolved, obtains
Ammonia solvent liquid, the 3rd defecator is used to carry out ammonia solvent liquid the 5th filtration, the filter being filtrated to get for the 5th time
Liquid is ammonium paratungstate and/or ammonium molybdate solution, and filtering residue is ammonium metavanadate solid.
Preferably, the device that is pulverized and mixed is including disintegrating machine, flour mill and blender, the disintegrating machine, flour mill and
Blender is sequentially connected by pipeline.
Preferably, bucket elevator, the disintegrating machine export pipeline are provided between the disintegrating machine and the flour mill
It is connected with the entrance of the bucket elevator bottom, the outlet on the bucket elevator top and the entrance pipe of the flour mill
Connection.
Preferably, batcher, the flour mill export pipeline and institute are provided between the flour mill and the blender
The connection of batcher entrance is stated, the batcher outlet is connected with the entrance pipe of the blender.
Preferably, the batcher is spiral batcher.
Preferably, it is provided with the first delivery pump between first defecator and second storage device, described
The export pipeline of one defecator is connected with the entrance pipe of first delivery pump, the outlet of first delivery pump and institute
The entrance for stating the second storage device is connected.
Preferably, it is provided with the second delivery pump between second defecator and first storage device, described
The export pipeline of two defecators is connected with the entrance pipe of first delivery pump, the outlet of second delivery pump and institute
The entrance for stating the first storage device is connected, and second delivery pump is used for the filtrate of second filtration and returns to the first storage device
Middle recycling.
Preferably, the export pipeline connection of the 3rd defecator is connected with the entrance pipe of the 3rd delivery pump, described
3rd delivery pump is used for the filtrate output for being filtrated to get the 5th time.
Preferably, the calciner is rotary kiln.
Preferably, the disintegrating machine is jaw crusher, and the flour mill is Raymond mill.
Compared with prior art, a kind of SCR waste catalyst recoveries system described herein, has reached following effect：
(1) this utility model, was provided with before calciner and is pulverized and mixed device, by the mixed type roasting using optimization
Auxiliary agent is burnt, is sufficiently mixed device is pulverized and mixed, hence it is evident that improve the leaching rate of the valuable metals such as vanadium, tungsten (molybdenum), while reducing
The usage amount of auxiliary agent, so that soluble-salt concentration is very low in the filtrate that second is filtered in the second storage device, can
It is returned directly in the first storage device without process, cooks impregnation liquid recycling, significantly reduces water resources consumption and process energy
Consumption.
(2) this utility model, due to leachate vanadium, tungsten and/or molybdenum concentration it is very low, in the second storing in this utility model
In device it is enriched with first, substantial amounts of water is used in time in the first storage device and recycle, and follow up device
In purification process only a small amount of vanadium tungsten and/or molybdenum need to be processed, significantly reduce process load and additive dosage.
(3) this utility model, the second drawing mechanism therein, the second defecator, the 3rd drawing mechanism and the 3rd filter
Device arranges reasonable so that same device is used for multiple times, and improves utilization rate in a flow process.
(4) this utility model, structure composition is simple, is provided with the pipeline of many places recovery so that water consumption is low, auxiliary agent addition
Amount is less, post processing energy consumption is low and load is little.
Description of the drawings
Accompanying drawing described herein is used for providing further understanding to of the present utility model, constitutes of the present utility model one
Point, the schematic description and description of the present invention is used to explain this utility model, does not constitute to of the present utility model improper
Limit.In the accompanying drawings：
Fig. 1 is SCR waste catalyst recoveries method process chart of the present invention；
Fig. 2 is the structure diagram of SCR waste catalyst recoveries system of the present invention.
Specific embodiment
Description subsequent descriptions are to implement the better embodiment of the application, and so the description is to illustrate the one of the application
As for the purpose of principle, be not limited to scope of the present application.The protection domain of the application ought be defined depending on claims
Person is defined.
Some nouns in the application are described below：
G is mass unit gram；Ml is volume unit milliliter；DEG C be temperature unit degree Celsius；KJ is energy unit's Kilojoule；
Concentration of hydrochloric acid unit is grams per milliliter, and such as 8% hydrochloric acid refers to contain 8 grams of hydrogen chloride in 100 milliliters of dilute hydrochloric acid.
The application is described in further detail below in conjunction with accompanying drawing, but not as the restriction to the application.
Embodiment 1
(1) 5g sodium carbonate, 2g Sodium Chloride, 3g sodium nitrates is added to carry out powder with Raymond mill in 1000g SCR dead catalyst
It is broken with mix thoroughly, obtain compound；By the compound in Muffle furnace 1000 DEG C of roastings 1 hour, 8000ml deionizations are used after cooling
Water retting 1 hour is simultaneously filtered, and after filtering residue washing TiO is removed2Factory reclaims, can be used as production TiO2Raw material；
(3) 40g calcium chloride is added in the filtrate for obtaining, precipitation enrichment is carried out, is filtered, filtrate collection gets up, can conduct
The impregnation liquid of next roasting material；
(4) filtering residue for obtaining is to wash the impurity such as removing Calcium Carbonate, the pH value control of washing liquid for 1% dilute hydrochloric acid with 20ml concentration
System obtains washing liquid and precipitate 2～3 after washing；
(5) precipitate obtained after washing is impregnated and is dissolved with 60ml concentration for 8% hydrochloric acid, obtains lysate；It is molten
Solution liquid adjusts pH value to 2～3 with ammonia again, precipitation occurs, filters, and the filtrate for obtaining is merged with the washing liquid in washing step,
Purified recovery obtains calcium chloride, reclaims the calcium chloride for obtaining and returns to used in step (3)；
(6) ammonia that 80ml concentration is 25% is added in the filtering residue obtained in step (5), the part of dissolving is para-tungstic acid
Ammonium, insoluble part is ammonium metavanadate.
Embodiment 2
(1) 25g sodium carbonate, 10g Sodium Chloride, 15g sodium nitrates is added to be carried out with Raymond mill in 1000g SCR dead catalyst
Crush and mix thoroughly, obtain compound；By the compound in Muffle furnace 500 DEG C of roastings 5 hours, 1000ml deionizations are used after cooling
Water retting 5 hours is simultaneously filtered, and after filtering residue washing TiO is removed2Factory reclaims, can be used as production TiO2Raw material；
(3) 40g calcium chloride is added in the filtrate for obtaining, precipitation enrichment is carried out, is filtered, filtrate collection gets up, can conduct
The impregnation liquid of next roasting material；
(4) filtering residue for obtaining is that the impurity such as removing Calcium Carbonate are washed with the dilute hydrochloric acid of 90ml 1%, and the pH value of washing liquid is controlled 1
～2, washing liquid and precipitate are obtained after washing；
(5) precipitate obtained after washing is impregnated and is dissolved with 60ml concentration for 8% hydrochloric acid, obtains lysate, pH
Control is below 1；Lysate adjusts pH value to 4～5 with ammonia again, precipitation occurs, filters, by the filtrate for obtaining and washing step
In washing liquid merge, purified recovery obtains calcium chloride, reclaims the calcium chloride for obtaining and returns to used in step (3)；
(6) add 50ml concentration to be 28% ammonia solvent in the filtering residue obtained in step (5), filter, the filtrate for obtaining
For secondary tungsten acid ammonium solution, the filtering residue for obtaining is ammonium metavanadate solid.
Embodiment 3
(1) 100g sodium carbonate, 45g Sodium Chloride, 55g sodium nitrates is added to be entered with Raymond mill in 1000g SCR dead catalyst
Row is crushed and mixed thoroughly, obtains compound；By the compound in Muffle furnace 700 DEG C of roastings 5 hours, gone with 10000ml after cooling
Ion water retting 2 hours is simultaneously filtered, and after filtering residue washing TiO is removed2Factory reclaims, can be used as production TiO2Raw material；
(3) 35g calcium chloride is added in the filtrate for obtaining, precipitation enrichment is carried out, is filtered, filtrate collection gets up, can conduct
The impregnation liquid of next roasting material；
(4) filtering residue for obtaining is that the impurity such as removing Calcium Carbonate are washed with the dilute hydrochloric acid of 90ml 1%, and the pH value of washing liquid is controlled 2
～3, washing liquid and precipitate are obtained after washing；
(5) precipitate obtained after washing is impregnated and is dissolved with the hydrochloric acid of 70ml 7%, below, obtains lysate, pH
Control is below 1；Lysate adjusts pH value to 3～4 with ammonia again, precipitation occurs, filters, by the filtrate for obtaining and washing step
In washing liquid merge, purified recovery obtains calcium chloride, reclaims the calcium chloride for obtaining and returns to used in step (3)；
(6) ammonia is added in the filtering residue obtained in step (5), the part of dissolving is ammonium paratungstate, and insoluble part is inclined
Ammonium vanadate.
Embodiment 4
(1) 50g sodium carbonate, 25g Sodium Chloride, 25g sodium nitrates is added to be carried out with Raymond mill in 1000g SCR dead catalyst
Crush and mix thoroughly, obtain compound；
(2) by the compound in Muffle furnace 800 DEG C of roastings 2 hours, with 5000ml deionized water dippings 1 hour after cooling
And filter, remove TiO after filtering residue washing2Factory reclaims, can be used as production TiO2Raw material；
(3) 40g calcium chloride is added in the filtrate for obtaining, precipitation enrichment is carried out, is filtered, filtrate collection gets up, can conduct
The impregnation liquid of next roasting material；
(4) filtering residue for obtaining is to wash the impurity such as removing Calcium Carbonate, the pH value control of washing liquid for 1% dilute hydrochloric acid with 80ml concentration
System obtains washing liquid and precipitate 2～3 after washing；
(5) precipitate obtained after washing is impregnated and is dissolved with 80ml concentration for 8% hydrochloric acid, obtains lysate；It is molten
Solution liquid adjusts pH value to 2～3 with ammonia again, precipitation occurs, filters, and the filtrate for obtaining is merged with the washing liquid in washing step,
Purified recovery obtains calcium chloride, reclaims the calcium chloride for obtaining and returns to used in step (3)；
(6) ammonia that 80ml concentration is 25% is added in the filtering residue obtained in step (5), the part of dissolving is para-tungstic acid
Ammonium, insoluble part is ammonium metavanadate.
Embodiment 5
(1) 40g sodium carbonate, 20g Sodium Chloride, 20g sodium nitrates is added to be carried out with Raymond mill in 1000g SCR dead catalyst
Crush and mix thoroughly, obtain compound；
(2) by the compound in Muffle furnace 800 DEG C of roastings 2 hours, spending 5000ml last time after cooling leaches after enrichment
Filtrate recycle impregnate and 1 hour and filter, remove TiO after filtering residue washing2Factory reclaims, can be used as production TiO2Raw material；
(3) 40g calcium chloride is added in the filtrate for obtaining, precipitation enrichment is carried out, is filtered, filtrate collection gets up, can conduct
The impregnation liquid of next roasting material；
(4) filtering residue for obtaining is that the impurity such as removing Calcium Carbonate are washed with the dilute hydrochloric acid of 60ml 1%, and the pH value of washing liquid is controlled 2
～3, washing liquid and precipitate are obtained after washing；
(5) precipitate obtained after washing is impregnated and is dissolved with the hydrochloric acid of 70ml 7%, obtains lysate；Lysate is again
PH value being adjusted to 2～3, precipitation occur, filtered, the filtrate for obtaining is merged with the washing liquid in washing step with ammonia, it is purified
Recovery obtains calcium chloride, reclaims the calcium chloride for obtaining and returns to used in step (3)；
(6) 60ml ammonia is added in the filtering residue obtained in step (5), is filtered, the filtrate for obtaining is secondary tungsten acid ammonium solution,
The filtering residue for obtaining is ammonium metavanadate solid.
Embodiment 6
(1) 50g sodium carbonate, 25g Sodium Chloride, 25g sodium nitrates is added to be carried out with Raymond mill in 1000g SCR dead catalyst
Crush and mix thoroughly, obtain compound；
(2) by the compound in Muffle furnace 600 DEG C of roastings 1 hour, leached after enrichment with 5000ml last time after cooling
Filtrate recycle impregnates 3 hours and filters, and after filtering residue washing TiO is removed2Factory reclaims, can be used as production TiO2Raw material；
(3) 40g calcium chloride is added in the filtrate for obtaining, precipitation enrichment is carried out, is filtered, filtrate collection gets up, can conduct
The impregnation liquid of next roasting material；
(4) filtering residue for obtaining is to wash the impurity such as removing Calcium Carbonate, the pH value control of washing liquid for 1% dilute hydrochloric acid with 50ml concentration
System obtains washing liquid and precipitate 4～5 after washing；
(5) precipitate obtained after washing is impregnated and is dissolved with 60ml concentration for 8% hydrochloric acid, obtains lysate, pH
Control is below 1；Lysate adjusts pH value to 4～5 with ammonia again, precipitation occurs, filters, by the filtrate for obtaining and washing step
In washing liquid merge, purified recovery obtains calcium chloride, reclaims the calcium chloride for obtaining and returns to used in step (3)；
(6) add 50ml concentration to be 28% ammonia solvent in the filtering residue obtained in step (5), filter, the filtrate for obtaining
For secondary tungsten acid ammonium solution, the filtering residue for obtaining is ammonium metavanadate solid.
Embodiment 7
(1) 50g sodium carbonate, 25g Sodium Chloride, 25g sodium nitrates is added to be carried out with Raymond mill in 1000g SCR dead catalyst
Crush and mix thoroughly, obtain compound；
(2) by the compound in Muffle furnace 700 DEG C of roastings 2 hours, leached after enrichment with 5000ml last time after cooling
Filtrate recycle impregnates 4 hours and filters, and after filtering residue washing TiO is removed2Factory reclaims, can be used as production TiO2Raw material；
(3) 25g calcium chloride is added in the filtrate for obtaining, precipitation enrichment is carried out, is filtered, filtrate collection gets up, can conduct
The impregnation liquid of next roasting material；
(4) filtering residue for obtaining is to wash the impurity such as removing Calcium Carbonate, the pH value control of washing liquid for 1% dilute hydrochloric acid with 40ml concentration
System obtains washing liquid and precipitate 2～3 after washing；
(5) precipitate obtained after washing is impregnated and is dissolved with 50ml concentration for 7% hydrochloric acid, obtains lysate；It is molten
Solution liquid adjusts pH value to 1～2 with ammonia again, precipitation occurs, filters, and the filtrate for obtaining is merged with the washing liquid in washing step,
Purified recovery obtains calcium chloride, reclaims the calcium chloride for obtaining and returns to used in step (3)；
(6) ammonia that 40ml concentration is 28% is added in the filtering residue obtained in step (5), the part of dissolving is para-tungstic acid
Ammonium, insoluble part is ammonium metavanadate.
Embodiment 8
The present embodiment is traditional method, without the contrast in the present invention
(1) add 500g sodium carbonate to be crushed with Raymond mill and mixed thoroughly in 1000g SCR dead catalyst, mixed
Material；By the compound in Muffle furnace 700 DEG C of roastings 5 hours, with 5000ml deionized water dippings 5 hours and filter after cooling,
TiO is removed after filtering residue washing2Factory reclaims, can be used as production TiO2Raw material；
(2) 1800g ammonium chloride is added in the filtrate obtained in step (1), there is Precipitation, be filtrated to get metavanadic acid
Ammonium.
(3) 40g calcium chloride is added in the filtrate obtained to step (2), precipitation is filtered out and is obtained artificial schellite, filtrate Jing evaporations
Ammonium chloride and water are obtained, water can be back to dipping process.
(5) artificial schellite for obtaining is impregnated with 50ml concentration for 7% hydrochloric acid, and the precipitation after filtration is with 40ml concentration
28% ammonia solvent obtains ammonium paratungstate.
Table 1
The data such as the recovering effect and auxiliary dosage and energy consumption of enforcement row 1～8 are given in table 1, wherein auxiliary dosage refers to
Be sodium carbonate, Sodium Chloride, sodium nitrate and calcium chloride；Wherein the leaching liquid of embodiment 8 without step in the present invention (3) richness
Collection, but later separation is directly carried out, its process load is larger, in order to the ammonium vanadate that settles out needs to add substantial amounts of ammonium chloride to try
Agent, and also contain a large amount of ammonium chloride in filtrate thereafter, and directly the solution can not be back to into leaching operation next time, lead
Substantial amounts of wastewater problem is caused.The process for carrying out its reuse is such as needed to result in very high energy consumption.
In above-described embodiment, SCR dead catalyst used is the catalyst for not containing molybdenum, in the SCR dead catalyst having
Molybdenum can be contained, its recovery method is same as the previously described embodiments, simply wherein the recovery of molybdenum is identical with the recovery state of tungsten, i.e., in step
Suddenly molybdenum is present as a solution in (6).Will not be described here.
Embodiment 9
The present embodiment provides the system used by the method for the SCR waste catalyst recoveries in embodiment 1-7, such as Fig. 2 institutes
Show, a kind of SCR waste catalyst recoveries system, including be sequentially connected be pulverized and mixed device, calciner, the first storage device,
First defecator, the second storage device, the second defecator, the 3rd storage device and the 3rd defecator；
As shown in Fig. 2 the wherein described device that is pulverized and mixed is including disintegrating machine 1, the export pipeline of disintegrating machine 1 is connected to bucket type
The import of elevator 2, the export pipeline of bucket elevator 2 is connected to the entrance of flour mill 3, the export pipeline connection of flour mill 3
To the entrance of screw(-type) feeder 4, the export pipeline of screw(-type) feeder 4 is connected with the entrance of blender 7, the export pipeline of blender 7 with
The entrance of calcining kiln 8 connects；
The export pipeline of calcining kiln 8 is connected with the entrance of the first storage device 9, the export pipeline and first of the first storage device 9
The entrance of defecator 10 connects, and the filtering residue of the first defecator 10 is TiO2, the filtrate (liquid pipeline of the first defecator 10 process
First delivery pump 11 is connected with the entrance of the second storage device 12, the export pipeline of the second storage device 12 and the second defecator 13
Entrance connects, the filtering residue of the second defecator 13, and the filtrate (liquid pipeline of the second defecator 13 is through the second delivery pump 14 and the
The entrance pipe connection of one drawing mechanism 10；
The sludge outlet of the second defecator 13 is connected with the entrance of the 3rd storage device 15, and the 3rd storage device 15 is exported
Pipeline is connected with the entrance of the 3rd defecator 16, the filtrate (liquid and sludge outlet of the 3rd defecator 16, and the 3rd filters dress
The 3rd delivery pump 17 is connected with after the filtrate (liquid for putting 16.
The concrete processing procedure of said system is as follows：First SCR dead catalyst and roasting auxiliary agent carry out powder in pulverizer 1
Broken, the material after crushing enters bucket elevator 2 through the export pipeline of pulverizer 1, carries in mixture through bucket elevator 2
Eminence is raised to, through the export pipeline of bucket elevator 2 flour mill 3, outlet of the material after pulverizing from flour mill are entered
Pipeline enters the entrance of screw(-type) feeder 4, and the material after pulverizing is conveyed to blender 7 by screw(-type) feeder 4, and in blender 7
In sufficiently mixed；Material after mix homogeneously enters calcining kiln 8 through the export pipeline of blender 7, enters in calcining kiln
Row roasting；
Material after roasting enters the first storage device 9 by the export pipeline of calcining kiln, in the first storage device 9
Deionized water impregnates to the material after roasting, after dipping is completed, by the export pipeline of the first storage device 9 the is entered
Material after dipping is carried out first time filtration by one defecator 10, the first defecator 10, and filtering residue washing recovery is obtained
TiO2；The filtrate being filtrated to get for the first time enters the second storage device 12 through the first delivery pump 11；
Calcium chloride is added to the filtrate that the first time in the second storage device 12 filters, precipitation enrichment is carried out；Precipitation enrichment
Afterwards the export pipeline through the second storage device 12 enters the second defecator 13, the thing after the enrichment of the second defecator 13 pairs
Material carries out second filtration, and second resulting filter liquor enters the first storage device 9 through the second delivery pump, for the second time
Filter liquor is reclaimed for impregnating, and second filtration filtering residue returns to the second storage device 13；
Second storage device 13 pairs second filters filtering residue and is washed with dilute hydrochloric acid, and the material after washing enters the second mistake
Filter device 13, the material after the second defecator 13 is washed carries out the 3rd filtration, the filtrate filtering residue being filtrated to get for the third time；3rd
The filtering residue of secondary filtration enters the 3rd storage device 15；
3rd storage device 15 carries out dipping dissolving with hydrochloric acid to the filtering residue that third time is filtrated to get, and obtains lysate, to
Add ammonia to adjust the pH value of lysate in 3rd storage device 15, be precipitated；Material after precipitation is through the 3rd storing
The export pipeline of device 15 enters the 3rd defecator 16, and the material after the 3rd defecator 16 pairs precipitation carries out the 4th mistake
Filter, obtains filtrate and the filtering residue of the 4th filtration, and the filtrate that the 4th filtrate filtered obtains with third time merges recovery calcium chloride, the
The filtering residue being filtrated to get for four times returns to the 3rd storage device 16；
The filtering residue ammonia solvent that 3rd storage device 16 pairs is filtrated to get for the 4th time, filtering residue is partly dissolved, is partly dissolved
Material through the 3rd storage device 15 export pipeline enter the 3rd defecator 16, the 3rd defecator 16 is to ammonia solvent
Liquid carries out the 5th filtration, and the filtrate being filtrated to get for the 5th time is ammonium paratungstate and/or ammonium molybdate solution, is filtrated to get for the 5th time
Filtering residue be ammonium metavanadate solid ammonium metavanadate solid.
In certain embodiments, disintegrating machine can select jaw crusher, or impact breaker, vertical impact
Formula disintegrating machine, hydro cone-crusher, ring hammer crusher, hammer mill, kibbler roll, compound crusher, circular cone
Formula disintegrating machine, twin-stage disintegrating machine, gyratory crusher, movable crusher etc..
In certain embodiments, flour mill can select Raymond mill, or longitudinal swinging pulverizer, high-pressure overhang roll pulverizing
Machine, high-pressure micronizer powder machine, straight-through centrifugal disintegrator powder machine, super-pressure trapezoidal pulverizing machine, three ring middling speed flour mills etc..
In certain embodiments, calciner can select rotary kiln, or reverberatory furnace, multiple hearth furnace, shaft furnace, boiling
Stove, apply wind furnace etc..
In certain embodiments, the first storage device, the second storage device and/or the 3rd storage device can be tied for cell body
Structure, tank structure and other reactors etc. also can be used.
In certain embodiments, the first defecator, the second defecator and/or the 3rd defecator can be de- for centrifugation
Water dispenser, and other common defecators.
Compared with prior art, a kind of SCR waste catalyst recoveries system described in the utility model, has reached following effect
Really：
(1) this utility model, was provided with before calciner and is pulverized and mixed device, by the mixed type roasting using optimization
Auxiliary agent is burnt, is sufficiently mixed device is pulverized and mixed, hence it is evident that improve the leaching rate of the valuable metals such as vanadium, tungsten (molybdenum), while reducing
The usage amount of auxiliary agent, so that soluble-salt concentration is very low in the filtrate that second is filtered in the second storage device, can
It is returned directly in the first storage device without process, cooks impregnation liquid recycling, significantly reduces water resources consumption and process energy
Consumption.
(2) this utility model, due to leachate vanadium, tungsten and/or molybdenum concentration it is very low, in the second storing in this utility model
In device it is enriched with first, substantial amounts of water is used in time in the first storage device and recycle, and follow up device
In purification process only a small amount of vanadium tungsten and/or molybdenum need to be processed, significantly reduce process load and additive dosage.
(3) this utility model, the second drawing mechanism therein, the second defecator, the 3rd drawing mechanism and the 3rd filter
Device arranges reasonable so that same device is used for multiple times, and improves utilization rate in a flow process.
(4) this utility model, structure composition is simple, is provided with the pipeline of many places recovery so that water consumption is low, auxiliary agent addition
Amount is less, post processing energy consumption is low and load is little.
Because method part has been described in detail to the embodiment of the present application, the system to being related in embodiment here
Expansion description with method corresponding part is omitted, and is repeated no more.Implement for the description of particular content in system refers to method
The content of example, no longer specifically limits here.
Described above illustrates and describes some preferred embodiments of the application, but as previously mentioned, it should be understood that the application
Be not limited to form disclosed herein, be not to be taken as the exclusion to other embodiment, and can be used for various other combinations,
Modification and environment, and can be in application contemplated scope described herein, by above-mentioned teaching or the technology or knowledge of association area
It is modified.And change that those skilled in the art are carried out and change be without departing from spirit and scope, then all should be in this Shen
Please be in the protection domain of claims.
Claims (10)
1. a kind of SCR waste catalyst recoveries system, it is characterised in that described to be pulverized and mixed device use including device is pulverized and mixed
In SCR dead catalyst and roasting auxiliary agent are crushed, and mix homogeneously, obtain compound；
Described being pulverized and mixed after device is connected with calciner, and the calciner is used to carry out roasting to compound；
The first storage device is connected with after the calciner, first storage device is used to enter the compound after roasting
Row deionized water dipping, is connected with the first defecator after first storage device, first defecator is used for will
Material after dipping carries out first time filtration, and filtering residue washing recovery obtains TiO2；
First storage device is connected with the second storage device, and second storage device is used for the filtrate filtered to first time
Calcium chloride is added, precipitation enrichment is carried out；The second defecator is connected with after second storage device, described second filters dress
Put for carrying out second filtration to the material after enrichment, second resulting filter liquor is filled into first storing
Put, reclaim for impregnating, filtering residue returns to the second storage device；
Second storage device is used to carry out dilute hydrochloric acid washing to the second filtering residue for filtering, and second defecator is to described
Material after dilute hydrochloric acid washing carries out the 3rd filtration, the filtrate filtering residue being filtrated to get for the third time；
The 3rd storage device is connected with after second defecator, the 3rd storage device is used to filter third time
To filtering residue carry out salt acid dip dissolving and obtain lysate, ammonia adjusts the pH value of the lysate, is precipitated；It is described
The 3rd defecator is connected with after 3rd storage device, the 3rd defecator is used to carry out the 4th to the material after precipitation
Secondary filtration, obtains filtrate and the filtering residue of the 4th filtration, and the filtrate that the 4th filtrate filtered obtains with third time merges recovery chlorination
Calcium, the filtering residue being filtrated to get for the 4th time returns to the 3rd storage device；
3rd storage device is used for the filtering residue ammonia solvent being filtrated to get to the 4th time, and filtering residue is partly dissolved, and obtains ammonia
Lysate, the 3rd defecator is used to carry out ammonia solvent liquid the 5th filtration, and the filtrate being filtrated to get for the 5th time is
Ammonium paratungstate and/or ammonium molybdate solution, filtering residue is ammonium metavanadate solid.
2. SCR waste catalyst recoveries system according to claim 1, it is characterised in that the device that is pulverized and mixed includes
Disintegrating machine, flour mill and blender, the disintegrating machine, flour mill and blender are sequentially connected by pipeline.
3. SCR waste catalyst recoveries system according to claim 2, it is characterised in that the disintegrating machine and the pulverizing
Bucket elevator is provided between machine, the disintegrating machine export pipeline is connected with the entrance of the bucket elevator bottom, described
The outlet on bucket elevator top is connected with the entrance pipe of the flour mill.
4. SCR waste catalyst recoveries system according to claim 3, it is characterised in that the flour mill and the mixing
Batcher is provided between device, the flour mill export pipeline is connected with the batcher entrance, the batcher is exported and institute
State the entrance pipe connection of blender.
5. SCR waste catalyst recoveries system according to claim 4, it is characterised in that the batcher is spirally to give
Material machine.
6. SCR waste catalyst recoveries system according to claim 5, it is characterised in that first defecator and institute
State and the first delivery pump is provided between the second storage device, the export pipeline of first defecator and first delivery pump
Entrance pipe be connected, the outlet of first delivery pump is connected with the entrance of second storage device.
7. SCR waste catalyst recoveries system according to claim 6, it is characterised in that second defecator and institute
State and the second delivery pump is provided between the first storage device, the export pipeline of second defecator and first delivery pump
Entrance pipe be connected, the outlet of second delivery pump is connected with the entrance of first storage device, and described second is defeated
Send pump and return in the first storage device recycling for second filtrate filtered.
8. SCR waste catalyst recoveries system according to claim 7, it is characterised in that the 3rd defecator goes out
Mouth pipeline connection is connected with the entrance pipe of the 3rd delivery pump, and the 3rd delivery pump is used for the filtrate for being filtrated to get the 5th time
Output.
9. SCR waste catalyst recoveries system according to claim 8, it is characterised in that the calciner is rotary kiln.
10. SCR waste catalyst recoveries system according to claim 2, it is characterised in that the disintegrating machine is broken for Hubei Province formula
Machine, the flour mill is Raymond mill.
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| CN201621035288.7U CN206104533U (en) | 2016-08-31 | 2016-08-31 | SCR dead catalyst recovery system |
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| CN201621035288.7U CN206104533U (en) | 2016-08-31 | 2016-08-31 | SCR dead catalyst recovery system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114433598A (en) * | 2022-02-14 | 2022-05-06 | 季秀女 | Treatment method of electrolytic aluminum |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114433598A (en) * | 2022-02-14 | 2022-05-06 | 季秀女 | Treatment method of electrolytic aluminum |
| CN114433598B (en) * | 2022-02-14 | 2024-05-03 | 巩义新格新材料有限公司 | Electrolytic aluminum treatment method |
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