CN108655157B - It is a kind of for changing the detoxification treatment process of blacklead - Google Patents
It is a kind of for changing the detoxification treatment process of blacklead Download PDFInfo
- Publication number
- CN108655157B CN108655157B CN201810440900.6A CN201810440900A CN108655157B CN 108655157 B CN108655157 B CN 108655157B CN 201810440900 A CN201810440900 A CN 201810440900A CN 108655157 B CN108655157 B CN 108655157B
- Authority
- CN
- China
- Prior art keywords
- level
- liquid
- solid
- blacklead
- sent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 32
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 238000001784 detoxification Methods 0.000 title claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 59
- 238000006243 chemical reaction Methods 0.000 claims abstract description 37
- 239000000243 solution Substances 0.000 claims abstract description 28
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000007787 solid Substances 0.000 claims abstract description 20
- 230000007062 hydrolysis Effects 0.000 claims abstract description 15
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 15
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 11
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 10
- 238000007599 discharging Methods 0.000 claims abstract description 10
- 238000001704 evaporation Methods 0.000 claims abstract description 10
- 230000008020 evaporation Effects 0.000 claims abstract description 10
- UMPKMCDVBZFQOK-UHFFFAOYSA-N potassium;iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[K+].[Fe+3] UMPKMCDVBZFQOK-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000004411 aluminium Substances 0.000 claims abstract description 8
- 239000006228 supernatant Substances 0.000 claims abstract description 8
- 239000003337 fertilizer Substances 0.000 claims abstract description 6
- YADSGOSSYOOKMP-UHFFFAOYSA-N lead dioxide Inorganic materials O=[Pb]=O YADSGOSSYOOKMP-UHFFFAOYSA-N 0.000 claims abstract description 5
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000004021 humic acid Substances 0.000 claims abstract description 4
- 238000002347 injection Methods 0.000 claims abstract description 4
- 239000007924 injection Substances 0.000 claims abstract description 4
- 238000002156 mixing Methods 0.000 claims abstract 2
- 239000003513 alkali Substances 0.000 claims description 12
- 229920002521 macromolecule Polymers 0.000 claims description 12
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 8
- 238000011010 flushing procedure Methods 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- RVPVRDXYQKGNMQ-UHFFFAOYSA-N lead(2+) Chemical compound [Pb+2] RVPVRDXYQKGNMQ-UHFFFAOYSA-N 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- 238000012271 agricultural production Methods 0.000 claims description 4
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 4
- 230000003311 flocculating effect Effects 0.000 claims description 4
- 239000007836 KH2PO4 Substances 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 229910000402 monopotassium phosphate Inorganic materials 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- GNSKLFRGEWLPPA-UHFFFAOYSA-M potassium dihydrogen phosphate Chemical compound [K+].OP(O)([O-])=O GNSKLFRGEWLPPA-UHFFFAOYSA-M 0.000 claims description 3
- 239000002244 precipitate Substances 0.000 claims description 3
- 230000000717 retained effect Effects 0.000 claims description 3
- 239000013049 sediment Substances 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 239000002253 acid Substances 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract description 2
- 238000004062 sedimentation Methods 0.000 abstract 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract 1
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- 239000012141 concentrate Substances 0.000 abstract 1
- 238000009776 industrial production Methods 0.000 abstract 1
- 239000011574 phosphorus Substances 0.000 abstract 1
- 229910052698 phosphorus Inorganic materials 0.000 abstract 1
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 7
- 239000003380 propellant Substances 0.000 description 5
- 229910019142 PO4 Inorganic materials 0.000 description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 3
- SNIOPGDIGTZGOP-UHFFFAOYSA-N Nitroglycerin Chemical compound [O-][N+](=O)OCC(O[N+]([O-])=O)CO[N+]([O-])=O SNIOPGDIGTZGOP-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000005904 alkaline hydrolysis reaction Methods 0.000 description 2
- WPUINVXKIPAAHK-UHFFFAOYSA-N aluminum;potassium;oxygen(2-) Chemical compound [O-2].[O-2].[Al+3].[K+] WPUINVXKIPAAHK-UHFFFAOYSA-N 0.000 description 2
- -1 dimethyl acardite Chemical compound 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229960003711 glyceryl trinitrate Drugs 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 230000001376 precipitating effect Effects 0.000 description 2
- 238000009987 spinning Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- VNVCVUGYDCNJTE-UHFFFAOYSA-N C1=CC=C(C(=C1)C(=O)[Pb])N Chemical compound C1=CC=C(C(=C1)C(=O)[Pb])N VNVCVUGYDCNJTE-UHFFFAOYSA-N 0.000 description 1
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 1
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 239000000020 Nitrocellulose Substances 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- AZFNGPAYDKGCRB-XCPIVNJJSA-M [(1s,2s)-2-amino-1,2-diphenylethyl]-(4-methylphenyl)sulfonylazanide;chlororuthenium(1+);1-methyl-4-propan-2-ylbenzene Chemical compound [Ru+]Cl.CC(C)C1=CC=C(C)C=C1.C1=CC(C)=CC=C1S(=O)(=O)[N-][C@@H](C=1C=CC=CC=1)[C@@H](N)C1=CC=CC=C1 AZFNGPAYDKGCRB-XCPIVNJJSA-M 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 238000005354 coacervation Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 description 1
- 229920001220 nitrocellulos Polymers 0.000 description 1
- 239000000618 nitrogen fertilizer Substances 0.000 description 1
- 125000000018 nitroso group Chemical group N(=O)* 0.000 description 1
- 230000001473 noxious effect Effects 0.000 description 1
- 239000002686 phosphate fertilizer Substances 0.000 description 1
- 229940072033 potash Drugs 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 235000015320 potassium carbonate Nutrition 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 235000011181 potassium carbonates Nutrition 0.000 description 1
- 235000010333 potassium nitrate Nutrition 0.000 description 1
- 239000004323 potassium nitrate Substances 0.000 description 1
- 235000010289 potassium nitrite Nutrition 0.000 description 1
- 239000004304 potassium nitrite Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 1
- 229910052683 pyrite Inorganic materials 0.000 description 1
- 239000011028 pyrite Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000002341 toxic gas Substances 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- 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
- Y02W30/82—Recycling of waste of electrical or electronic equipment [WEEE]
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Fertilizers (AREA)
Abstract
It is a kind of for changing the detoxification treatment process of blacklead, the blacklead that changes scrapped is sent into liquid-solid reactor through the lock hopper at the top of lock hopper formula liquid-solid reactor, deenergize hydrolysis with the KOH solution counter current contacting ejected in lye injection pipe, reaction solution enters level-one from the discharge port of reactor and pond is mixed, and aluminium removal KH is added2PO4Reaction, reaction solution pass through level-one cyclone hydraulic separators for the Al (OH) of generation3Sedimentation removal；Supernatant enters back into second level mixing pond and deleading agent potassium ferrate is added to be reacted, and reaction solution passes through second level cyclone hydraulic separators for the Fe (OH) of generation3And PbO2Sedimentation removal；The supernatant of second level cyclone hydraulic separators enters stripper, the organic matters such as benzene homologues are carried away by water vapour, tower reactor discharging is by being concentrated by evaporation, concentrate enters preparing pool and mixes with flushed residue, humic acid and phosphorus acid for adjusting pH is added, the discharging of preparing pool is used for industrial production directly as liquid fertilizer；The present invention, which realizes, scraps deenergize detoxification and the recycling environmental protection utilization that change blacklead.
Description
Technical field
The present invention relates to scrap propellant powder safe disposal and application technology as the second resource field, and in particular to one kind is black for changing
The detoxification treatment process of lead.
Background technique
Changing blacklead is one kind based on cellulose and nitroglycerine, and RDX is the propellant of high energy additive, both be can guarantee
Propellant energy with higher, and it is able to achieve the smokeless emission of propellant.Other than nitrocellulose, nitroglycerine and RDX,
Change and also added aluminium powder, dimethyl acardite and o-amino benzoyl lead plumbate in blacklead.Change blacklead using basic hydrolysis for what is scrapped
Method, replaced with hydroxyl scrap nitro or nitroso on ammunition at a certain temperature, reach the purpose deenergized.Buck
The substances such as the potassium nitrate, potassium nitrite and the potassium carbonate that generate in solution preocess can be used as nitrogenous fertilizer and potash fertilizer is used for agricultural production, with
The resource utilization of deenergizing for changing blacklead is scrapped in realization.
In addition, that scraps changes blacklead alkaline hydrolysis process also and can generate that potassium metaaluminate, plumbous acid potassium and benzene homologues etc. are toxic to be had
Evil substance is enriched in metal ion in crops if crops can directly be polluted by functioning as fertilizer without processing, so that
Threaten the health of the mankind.
Currently, being mainly the precipitation method, coacervation, absorption method and ion-exchange for the removal of lead ion.In recent years,
About the method using magnetic iron ore absorption, work well, but in natural troilite magnetic iron ore and pyrite separation
Process is comparatively laborious, heavy workload, limits its practical application.Industrially sulfide solution is mostly used to react generation with lead ion
Vulcanized lead precipitating, but sulfide inherently noxious material, such as vulcanized sodium can decompose in acid and generates toxic gas vulcanization
Hydrogen, being stained on skin can cause to burn, and have high toxicity to aquatile.Operation can be required so relatively high, be easy to draw
Send out peril.In addition, preferably being gone for the potassium metaaluminate and benzene homologues proposition that change the generation of blacklead alkaline hydrolysis process not yet
Except method.
Summary of the invention
In order to overcome the disadvantages of the above prior art, the object of the present invention is to provide a kind of for changing the detoxification of blacklead
Treatment process, realization scrap change blacklead propellant deenergize, detoxification, recycling environmental protection utilize.
In order to achieve the above object, the technical scheme adopted by the invention is as follows:
It is a kind of for changing the detoxification treatment process of blacklead, comprising the following steps:
The first step, to be processed scrapping change the top that blacklead is sent to lock hopper formula solid-liquid reaction device 2 via belt conveyor 1,
It is flowed into lock hopper formula solid-liquid reaction device 2 by level-one lock hopper, is 20% with the mass concentration ejected from lye injection pipe 23
KOH solution counter current contacting complete macromolecule alkali for hydrolysis, control lock hopper formula solid-liquid reaction device 2 in temperature be 90 DEG C, KOH solution adds
Enter amount and controlled with the mass ratio for changing blacklead additional amount in 5-7:1, the heat that macromolecule alkali for hydrolysis process releases passes through in collet
Heat transferring medium water is taken away；
Second step, macromolecule alkali for hydrolysis liquid are flowed out from 2 top export mouth of lock hopper formula solid-liquid reaction device, are sent into via the first pump 4
Pond 8 is mixed to level-one and remove reactive aluminum, macromolecule alkali for hydrolysis residual residue and part reaction solution from lock hopper formula solid-liquid reaction
The bottom discharge port of device 2 discharges, and is sent into solid-liquid separator 5 via screw conveyor 3, by 40 mesh in solid-liquid separator 5
Sieve 51 solid residue and reaction solution are separated, solid residue flows into washer 7, rushes via the vibration of vibrating screen panel 71
It washes, the solid residue after flushing flows into preparing pool 22；Flushing liquor in solid-liquid separator 5 in clear liquid and washer 7 passes through respectively
It is sent to level-one by the second pump 6 and third pump 12 and is mixed in pond 8；
Third step is mixed in pond 8 toward level-one and aluminium removal KH is added2PO4, operating condition is that every cubic metre of clear liquid is added
10g KH2PO4, temperature is 50 DEG C, stirring intensity 0.8kW/m3Liquid；Level-one be mixed pond 8 in reaction residual liquor via
4th pump 9 is sent to the top of level-one cyclone hydraulic separators 10, by settling Al (OH)3It precipitates from the bottom of level-one cyclone hydraulic separators 10
Portion's discharging, and supernatant is overflowed from the top of level-one cyclone hydraulic separators 10, is sent into second level via the 5th pump 11 and is mixed
Pond 13 removes the lead ion in reaction solution；
The feed inlet in pond 13 is mixed in second level with 30g/cm in 4th step2Ratio be added potassium ferrate (K2FeO4),
PH is controlled in 8-10, stirring intensity 0.9-1.2kW/m3Liquid；The reaction residual liquor in pond 13 is mixed via the in second level
Six pumps 14 are sent to the top of second level cyclone hydraulic separators 15, by flocculating setting Fe (OH)3And PbO2Sediment divides from second level spinning liquid
From 15 bottom discharge of device, and supernatant overflows at the top of second level cyclone hydraulic separators 15, is sent into stripper via the 7th pump 16
17 upper feed inlets；
5th step, the stripping fluid that stripper 17 uses is water vapour, and the water vapour that temperature is 240-250 DEG C is with 1.5m3/
The rate of min enters the feed liquid counter current contacting entered with tower top from the tower bottom of stripper 17, there is 99% benzene homologues with other
Machine object is enriched in the gas phase from the top discharge of stripper 17, is then stored in after condensation process in organic matter storage tank 18,
The discharging 50% of 17 tower bottom of stripper flows back into 17 tower top of stripper, and remaining 50% is sent to evaporation and concentration via the 8th pump 19
In tower 20；
6th step is concentrated by evaporation tower 20 using 140-150 DEG C of steam heating, and 60% moisture is steamed from tower top, so
After carry out condensation process；Evaporation concentrated solution discharges from tower bottom, is sent into preparing pool 22 via the 9th pump 21；It is pressed in preparing pool 22
Volume ratio is that humic acid is added in 7-8%, and phosphoric acid is added by pH value of solution and is adjusted to 7-7.5, and the solid residue flowed into washer 7 is mixed
It closes；The discharging of preparing pool 22 uses in agricultural production directly as liquid fertilizer.
Temperature control system is set in the lock hopper formula solid-liquid reaction device 2.
Sieve 51 in the solid-liquid separator 5 is to be obliquely installed, and inclination angle is 15 °, guarantees the solid being retained down
Particle is flowed out from discharge port.
Vibrating screen panel 71 in the washer 7 is front and back vibration, so that solid residue moves forward with vibration.
Overflow weir is all arranged in the feed inlet of the level-one cyclone hydraulic separators 10 and second level cyclone hydraulic separators 15, so that feed liquid
It can slowly flow into two cyclone hydraulic separators.
Compared with prior art, the invention has the benefit that
1, KH is utilized2PO4Aluminium ion is removed, not only adjustable solution ph, the PO added4 3-Phosphate fertilizer is also used as,
Reduce the dosage of conditioning tank phosphoric acid.
2, lead ion is removed using potassium ferrate, avoids the use of sulfide, reduce dangerous generation in operating process
A possibility that.
3, using organic matters such as steam stripping removal benzene homologues, so that thering is enough water to deposit always in stripper 17
It ensure that the safety of operating process.
4, lead element removal is placed on behind aluminium element removal, avoids and adjusts pH repeatedly, and in removal lead element
During the potassium ferrate that adds can generate the Fe (OH) of Fe (III) and adsorption function with excellent flocculating function3, not only
It can help PbO2Precipitating, complete Al (OH) will can not also be precipitated in the last stage3Further precipitating increases aluminium element
Removal rate.
Detailed description of the invention
Fig. 1 is the flow diagram of present invention process.
Specific embodiment
Present invention will be further explained below with reference to the attached drawings and examples.
It is referring to Fig.1, a kind of for changing the detoxification treatment process of blacklead, comprising the following steps:
The first step, to be processed scrapping change the top that blacklead is sent to lock hopper formula solid-liquid reaction device 2 via belt conveyor 1,
It is flowed into lock hopper formula solid-liquid reaction device 2 by level-one lock hopper, is 20% with the mass concentration ejected from lye injection pipe 23
KOH solution counter current contacting complete macromolecule alkali for hydrolysis, in order to reach basic hydrolysis purpose, control in lock hopper formula solid-liquid reaction device 2
Temperature is 90 DEG C, and KOH solution additional amount is controlled with the mass ratio for changing blacklead additional amount in 5-7:1, the release of macromolecule alkali for hydrolysis process
Heat out is taken away by the heat transferring medium water in collet；
Second step, macromolecule alkali for hydrolysis liquid are flowed out from 2 top export mouth of lock hopper formula solid-liquid reaction device, are sent into via the first pump 4
Pond 8 is mixed to level-one and remove reactive aluminum, macromolecule alkali for hydrolysis residual residue and part reaction solution from lock hopper formula solid-liquid reaction
The bottom discharge port of device 2 discharges, and is sent into solid-liquid separator 5 via screw conveyor 3, by 40 mesh in solid-liquid separator 5
Sieve 51 solid residue and reaction solution are separated, solid residue flows into washer 7, rushes via the vibration of vibrating screen panel 71
It washes, the solid residue after flushing flows into preparing pool 22；Flushing liquor in solid-liquid separator 5 in clear liquid and washer 7 passes through respectively
It is sent to level-one by the second pump 6 and third pump 12 and is mixed in pond 8；
Third step is mixed in pond 8 toward level-one and aluminium removal KH is added2PO4, operating condition is that every cubic metre of clear liquid is added
10g KH2PO4, temperature is 50 DEG C, stirring intensity 0.8kW/m3Liquid；Level-one be mixed pond 8 in reaction residual liquor via
4th pump 9 is sent to the top of level-one cyclone hydraulic separators 10, by settling Al (OH)3It precipitates from the bottom of level-one cyclone hydraulic separators 10
Portion's discharging, and supernatant is overflowed from the top of level-one cyclone hydraulic separators 10, is sent into second level via the 5th pump 11 and is mixed
Pond 13 removes the lead ion in reaction solution；
The feed inlet in pond 13 is mixed in second level with 30g/cm in 4th step2Ratio be added potassium ferrate (K2FeO4),
PH is controlled in 8-10, stirring intensity 0.9-1.2kW/m3Liquid；The reaction residual liquor in pond 13 is mixed via the in second level
Six pumps 14 are sent to the top of second level cyclone hydraulic separators 15, by flocculating setting Fe (OH)3And PbO2Sediment divides from second level spinning liquid
From 15 bottom discharge of device, and supernatant overflows at the top of second level cyclone hydraulic separators 15, is sent into stripper via the 7th pump 16
17 upper feed inlets；
5th step, the stripping fluid that stripper 17 uses is water vapour, and the water vapour that temperature is 240-250 DEG C is with 1.5m3/
The rate of min enters the feed liquid counter current contacting entered with tower top from the tower bottom of stripper 17, there is 99% benzene homologues with other
Machine object is enriched in the gas phase from the top discharge of stripper 17, is then stored in after condensation process in organic matter storage tank 18,
The discharging 50% of 17 tower bottom of stripper flows back into 17 tower top of stripper, and remaining 50% is sent to evaporation and concentration via the 8th pump 19
In tower 20；
6th step is concentrated by evaporation tower 20 using 140-150 DEG C of steam heating, and 60% moisture is steamed from tower top, so
After carry out condensation process；Evaporation concentrated solution discharges from tower bottom, is sent into preparing pool 22 via the 9th pump 21；It is pressed in preparing pool 22
Volume ratio is that humic acid is added in 7-8%, and phosphoric acid is added by pH value of solution and is adjusted to 7-7.5, and the solid residue flowed into washer 7 is mixed
It closes；The discharging of preparing pool 22 uses in agricultural production directly as liquid fertilizer.
Temperature control system is set in the lock hopper formula solid-liquid reaction device 2, so that reaction temperature control is at 90 DEG C.
Sieve 51 in the solid-liquid separator 5 is to be obliquely installed, and inclination angle is 15 °, guarantees the solid being retained down
Particle can be flowed out from discharge port.
Vibrating screen panel 71 in the washer 7 is front and back vibration, so that solid residue moves forward with vibration.
Overflow weir is all arranged in the feed inlet of the level-one cyclone hydraulic separators 10 and second level cyclone hydraulic separators 15, so that feed liquid
It can slowly flow into two cyclone hydraulic separators.
Claims (5)
1. a kind of for changing the detoxification treatment process of blacklead, which comprises the following steps:
The first step, to be processed scrapping change the top that blacklead is sent to lock hopper formula solid-liquid reaction device (2) via belt conveyor (1),
It is flowed into lock hopper formula solid-liquid reaction device (2) by level-one lock hopper, is with the mass concentration ejected from lye injection pipe (23)
20% KOH solution counter current contacting completes macromolecule alkali for hydrolysis, and the temperature in control lock hopper formula solid-liquid reaction device (2) is 90 DEG C, KOH
Solution additional amount is controlled with the mass ratio for changing blacklead additional amount in 5-7:1, and the heat that macromolecule alkali for hydrolysis process releases passes through folder
Heat transferring medium water in set is taken away；
Second step, macromolecule alkali for hydrolysis liquid are sent into from export mouth outflow at the top of lock hopper formula solid-liquid reaction device (2) via the first pump (4)
Pond (8) are mixed to level-one to carry out except reactive aluminum, macromolecule alkali for hydrolysis residual residue and part reaction solution are anti-from lock hopper formula solid-liquid
It answers the bottom discharge port of device (2) to discharge, is sent into solid-liquid separator (5) via screw conveyor (3), by solid-liquid separator
(5) sieve (51) of 40 mesh in separates solid residue and reaction solution, and solid residue flows into washer (7), via vibration
The vibration of sieve (71) is rinsed, and the solid residue after flushing flows into preparing pool (22)；The interior clear liquid of solid-liquid separator (5) and flushing
Flushing liquor in machine (7) is sent to level-one via the second pump (6) and third pump (12) respectively and is mixed in pond (8)；
Third step is mixed in pond (8) toward level-one and aluminium removal KH is added2PO4, operating condition is that 10g is added in every cubic metre of clear liquid
KH2PO4, temperature is 50 DEG C, stirring intensity 0.8kW/m3Liquid；The reaction residual liquor in pond (8) is mixed via the in level-one
Four pumps (9) are sent to the top of level-one cyclone hydraulic separators (10), by settling Al (OH)3It precipitates from level-one cyclone hydraulic separators (10)
Bottom discharge, and supernatant overflows at the top of level-one cyclone hydraulic separators (10), is sent into second level via the 5th pump (11)
The lead ion in pond (13) removal reaction solution is mixed；
The feed inlet of pond (13) is mixed in second level with 30g/cm in 4th step2Ratio be added potassium ferrate (K2FeO4), pH
Control is in 8-10, stirring intensity 0.9-1.2kW/m3Liquid；The reaction residual liquor in pond (13) is mixed via the in second level
Six pumps (14) are sent to the top of second level cyclone hydraulic separators (15), by flocculating setting Fe (OH)3And PbO2Sediment is revolved from second level
Liquid/gas separator (15) bottom discharge, and supernatant overflows at the top of second level cyclone hydraulic separators (15), via the 7th pump (16)
It is sent into stripper (17) upper feed inlet；
5th step, the stripping fluid that stripper (17) uses is water vapour, and the water vapour that temperature is 240-250 DEG C is with 1.5m3/min
Rate enter the feed liquid counter current contacting that enters with tower top from the tower bottom of stripper (17), keep 99% benzene homologues organic with other
Object is enriched in the gas phase from the top discharge of stripper (17), and organic matter storage tank (18) are then stored in after condensation process
In, the discharging 50% of stripper (17) tower bottom flows back into stripper (17) tower top, and remaining 50% is sent into via the 8th pump (19)
Into evaporation and concentration tower (20)；
6th step is concentrated by evaporation the steam heating that tower (20) use 140-150 DEG C, and 60% moisture is steamed from tower top, then
Carry out condensation process；Evaporation concentrated solution discharges from tower bottom, is sent into preparing pool (22) via the 9th pump (21)；Toward preparing pool (22)
Humic acid inside is added for 7-8% by volume, phosphoric acid is added by pH value of solution and is adjusted to 7-7.5, the solid flowed into washer (7)
Residue mixing；The discharging of preparing pool (22) uses in agricultural production directly as liquid fertilizer.
2. according to claim 1 a kind of for changing the detoxification treatment process of blacklead, it is characterised in that: the lock hopper formula
Temperature control system is set in solid-liquid reaction device (2).
3. according to claim 1 a kind of for changing the detoxification treatment process of blacklead, it is characterised in that: the solid-liquid point
It is to be obliquely installed from the sieve (51) in device (5), inclination angle is 15 °, guarantees that the solid particle being retained down is flowed out from discharge port.
4. according to claim 1 a kind of for changing the detoxification treatment process of blacklead, it is characterised in that: the washer
(7) vibrating screen panel (71) in is front and back vibration, so that solid residue moves forward with vibration.
5. according to claim 1 a kind of for changing the detoxification treatment process of blacklead, it is characterised in that: the level-one rotation
Overflow weir is all arranged in the feed inlet of liquid/gas separator (10) and second level cyclone hydraulic separators (15), and feed liquid is enabled slowly to flow into two
In a cyclone hydraulic separators.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810440900.6A CN108655157B (en) | 2018-05-10 | 2018-05-10 | It is a kind of for changing the detoxification treatment process of blacklead |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810440900.6A CN108655157B (en) | 2018-05-10 | 2018-05-10 | It is a kind of for changing the detoxification treatment process of blacklead |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108655157A CN108655157A (en) | 2018-10-16 |
| CN108655157B true CN108655157B (en) | 2019-05-07 |
Family
ID=63779046
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810440900.6A Active CN108655157B (en) | 2018-05-10 | 2018-05-10 | It is a kind of for changing the detoxification treatment process of blacklead |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108655157B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111072435B (en) * | 2019-12-18 | 2021-06-04 | 湖北航天技术研究院总体设计所 | Processing device and processing method for invalid propellant |
| CN111440050B (en) * | 2020-05-14 | 2021-04-09 | 西安交通大学 | Recovery process of high value-added medical intermediate of scrapped explosives and powders |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3778320A (en) * | 1972-06-20 | 1973-12-11 | Rockwell International Corp | Non-polluting disposal of explosives and propellants |
| CN1279623A (en) * | 1997-09-18 | 2001-01-10 | 联合讯号公司 | Demilitarization of chemical munitions |
| CN103408341A (en) * | 2013-08-14 | 2013-11-27 | 中国人民解放军济南军区72465部队 | Energy-containing material safe disposal and resource utilization method and system |
| CN107827684A (en) * | 2017-11-30 | 2018-03-23 | 西安交通大学 | A kind of TNT basic hydrolysis handling process |
| CN107876548A (en) * | 2017-11-30 | 2018-04-06 | 西安交通大学 | A kind of vehicle-mounted integral is scrapped ammunition and deenergized disposal of resources system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3513226B2 (en) * | 1994-06-06 | 2004-03-31 | 三菱重工業株式会社 | How to handle explosives and explosives |
-
2018
- 2018-05-10 CN CN201810440900.6A patent/CN108655157B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3778320A (en) * | 1972-06-20 | 1973-12-11 | Rockwell International Corp | Non-polluting disposal of explosives and propellants |
| CN1279623A (en) * | 1997-09-18 | 2001-01-10 | 联合讯号公司 | Demilitarization of chemical munitions |
| CN103408341A (en) * | 2013-08-14 | 2013-11-27 | 中国人民解放军济南军区72465部队 | Energy-containing material safe disposal and resource utilization method and system |
| CN107827684A (en) * | 2017-11-30 | 2018-03-23 | 西安交通大学 | A kind of TNT basic hydrolysis handling process |
| CN107876548A (en) * | 2017-11-30 | 2018-04-06 | 西安交通大学 | A kind of vehicle-mounted integral is scrapped ammunition and deenergized disposal of resources system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108655157A (en) | 2018-10-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103351020B (en) | A kind of production method of basic copper chloride | |
| CN108706802B (en) | Treatment method and treatment system for pollutants generated by household garbage incineration | |
| US10682641B2 (en) | Ion exchange process | |
| CN101863600A (en) | Method for removing heavy metals from activated sludge | |
| CN112077128A (en) | Water washing treatment system and method for fly ash | |
| CN108655157B (en) | It is a kind of for changing the detoxification treatment process of blacklead | |
| CN212597897U (en) | Flying dust washing processing system | |
| CN113245342B (en) | Resource treatment method and treatment system for waste incineration fly ash water washing salt making based on seed crystal method | |
| CN107217135A (en) | A kind of method of the multistage Concentration of Gold Ag-Cu-Zn of cyanidation gold-extracted waste slag and synthetical recovery | |
| CN105217869A (en) | The method of resource of the spent acid produced in a kind of flue gas during smelting Sulphuric acid | |
| CN109264898A (en) | A kind of flying dust multistage dechlorination and water lotion decalcification softening process and its system | |
| CN110894113A (en) | Desulfurization wastewater dechlorination treatment method and desulfurization wastewater treatment equipment | |
| CN111889489A (en) | Treatment method and treatment system for aluminum electrolysis overhaul slag | |
| CN204874164U (en) | Zero release processing system of desulfurization waste water | |
| CN106186437A (en) | A kind of process technique producing the waste water manufacturing demineralized water generation in viscose rayon | |
| CN113526546B (en) | System and method for preparing battery-grade lead oxide through clean conversion of waste lead paste | |
| CN209583824U (en) | A kind of flying dust multistage dechlorination and water lotion decalcification melded system | |
| CN102241447A (en) | Process for separating calcium and magnesium ions from waste water containing manganese | |
| CN105384230B (en) | A kind of cellulose sewage pretreatment device and application | |
| CN108011147B (en) | Waste lead-acid storage battery treatment system, treatment process and application of secondary lead | |
| CN101545115A (en) | Method for producing electrolytic zinc from zinc oxide-containing materials | |
| CN112536156A (en) | Method for treating heavy metal in fly ash | |
| CN110382109A (en) | For processing the system and method for including the mineral of lanthanide series and producing rare earth oxide | |
| CN1074486A (en) | The chemical sorting method of wulfenite | |
| CN104986897B (en) | Method for recovering valuable metals in wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |