CN102815821A - Method for separating and recycling chrome-contained oxide waste liquid produced by oxidation and decoloration of lignite wax, deresination lignite wax, peat wax or deresination peat wax - Google Patents
Method for separating and recycling chrome-contained oxide waste liquid produced by oxidation and decoloration of lignite wax, deresination lignite wax, peat wax or deresination peat wax Download PDFInfo
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- CN102815821A CN102815821A CN2012102945251A CN201210294525A CN102815821A CN 102815821 A CN102815821 A CN 102815821A CN 2012102945251 A CN2012102945251 A CN 2012102945251A CN 201210294525 A CN201210294525 A CN 201210294525A CN 102815821 A CN102815821 A CN 102815821A
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- 239000007788 liquid Substances 0.000 title claims abstract description 93
- 239000002699 waste material Substances 0.000 title claims abstract description 74
- 239000001993 wax Substances 0.000 title claims abstract description 56
- 239000012187 peat wax Substances 0.000 title claims abstract description 53
- 230000003647 oxidation Effects 0.000 title claims abstract description 48
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000003077 lignite Substances 0.000 title abstract description 8
- 238000004064 recycling Methods 0.000 title abstract 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims abstract description 106
- 239000011651 chromium Substances 0.000 claims abstract description 103
- 229910052804 chromium Inorganic materials 0.000 claims abstract description 97
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 61
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 60
- 238000000502 dialysis Methods 0.000 claims abstract description 45
- 238000009792 diffusion process Methods 0.000 claims abstract description 44
- 230000009467 reduction Effects 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 12
- JOPOVCBBYLSVDA-UHFFFAOYSA-N chromium(6+) Chemical compound [Cr+6] JOPOVCBBYLSVDA-UHFFFAOYSA-N 0.000 claims abstract description 7
- MKYLOMHWHWEFCT-UHFFFAOYSA-N Manthidine Natural products C1C2=CC=3OCOC=3C=C2C2C3=CC(OC)C(O)CC3N1C2 MKYLOMHWHWEFCT-UHFFFAOYSA-N 0.000 claims description 47
- SNFRINMTRPQQLE-JQWAAABSSA-N Montanin Chemical compound O[C@H]([C@@]1(CO)O[C@H]1[C@H]1[C@H]2O3)[C@]4(O)C(=O)C(C)=C[C@H]4[C@]11OC3(CCCCCCCCCCC)O[C@@]2(C(C)=C)C[C@H]1C SNFRINMTRPQQLE-JQWAAABSSA-N 0.000 claims description 47
- SNFRINMTRPQQLE-OFGNMXNXSA-N Montanin Natural products O=C1[C@@]2(O)[C@@H](O)[C@@]3(CO)O[C@H]3[C@@H]3[C@H]4[C@@]5(C(=C)C)O[C@](CCCCCCCCCCC)(O4)O[C@@]3([C@H](C)C5)[C@@H]2C=C1C SNFRINMTRPQQLE-OFGNMXNXSA-N 0.000 claims description 47
- QTZPBQMTXNEKRX-UHFFFAOYSA-N Voacristine pseudoindoxyl Natural products N1C2=CC=C(OC)C=C2C(=O)C21CCN(C1)C3C(C(C)O)CC1CC32C(=O)OC QTZPBQMTXNEKRX-UHFFFAOYSA-N 0.000 claims description 47
- 235000010269 sulphur dioxide Nutrition 0.000 claims description 28
- 230000001590 oxidative effect Effects 0.000 claims description 21
- 235000011149 sulphuric acid Nutrition 0.000 claims description 21
- 239000001117 sulphuric acid Substances 0.000 claims description 21
- 238000005349 anion exchange Methods 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 239000004291 sulphur dioxide Substances 0.000 claims description 14
- 238000011084 recovery Methods 0.000 claims description 13
- 239000012528 membrane Substances 0.000 claims description 11
- 238000001914 filtration Methods 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 5
- GRWVQDDAKZFPFI-UHFFFAOYSA-H chromium(III) sulfate Chemical compound [Cr+3].[Cr+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O GRWVQDDAKZFPFI-UHFFFAOYSA-H 0.000 claims description 5
- 239000008187 granular material Substances 0.000 claims description 5
- 239000003208 petroleum Substances 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 230000003068 static effect Effects 0.000 claims description 2
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- 231100000419 toxicity Toxicity 0.000 abstract description 4
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- 239000012535 impurity Substances 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract 1
- 230000033116 oxidation-reduction process Effects 0.000 abstract 1
- 238000011946 reduction process Methods 0.000 abstract 1
- 238000001514 detection method Methods 0.000 description 6
- 239000000706 filtrate Substances 0.000 description 6
- 239000003153 chemical reaction reagent Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 210000004379 membrane Anatomy 0.000 description 2
- 239000003415 peat Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 235000019219 chocolate Nutrition 0.000 description 1
- KRVSOGSZCMJSLX-UHFFFAOYSA-L chromic acid Substances O[Cr](O)(=O)=O KRVSOGSZCMJSLX-UHFFFAOYSA-L 0.000 description 1
- 230000001684 chronic effect Effects 0.000 description 1
- 238000004040 coloring Methods 0.000 description 1
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- 238000010586 diagram Methods 0.000 description 1
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- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- AWJWCTOOIBYHON-UHFFFAOYSA-N furo[3,4-b]pyrazine-5,7-dione Chemical compound C1=CN=C2C(=O)OC(=O)C2=N1 AWJWCTOOIBYHON-UHFFFAOYSA-N 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
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- 210000002345 respiratory system Anatomy 0.000 description 1
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Abstract
The invention relates to a method for separating and recycling chrome-contained oxide waste liquid produced by oxidation and decoloration of lignite wax, deresination lignite wax, peat wax or deresination peat wax, and the method is characterized by utilizing the reducibility of sulfur dioxide (SO2) to reduce hexavalent chromium with strong toxicity in the chrome-contained oxide waste liquid produced by the oxidation and decoloration processing process of the lignite wax, deresination lignite wax, peat wax or deresination peat wax to trivalent chromium with small toxicity, and then the oxidation reduction liquid containing the trivalent chromium and the sulfuric acid in the chrome-contained oxide waste liquid are separated and recycled through the filter and diffusion dialysis. During the reduction and separation process, no foreign ion impurity is introduced, no phase change exists, no secondary pollution is caused, simplicity and convenience in operation can be realized, the device is simple, energy conservation and high efficiency can be realized, no emission and no pollution on the environment exist, the reutilization of the resource can be realized, and the pollution problem of the chrome-contained waste liquid field can be effectively solved.
Description
Technical field
The invention belongs to chrome waste liquid processing technology field in the chemical metallurgy, the separation and recovery method that contains chromium oxidation waste liquid that produces when relating to a kind of montanin wax, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration.
Background technology
In the raw ore of some brown coal, peat, be rich in montanin wax and peat wax, the extraction treatment of this brown coal, peat process organic solvent obtains montanin wax, deresination montanin wax, peat wax or deresination peat wax primary products; Primary products are the brown solid shape darkly, and added value is low when directly utilizing, and range of application is little; With the smart wax that can obtain light color after the processing of primary products oxidative decoloration; The smart wax Application Areas of light color is wide, and market demand is bigger, and added value is high.
Add man-hour in decolouring; Montanin wax, deresination montanin wax, peat wax or the deresination peat wax of chocolate are carried out heat fused respectively; The oxygenant that will decolour then is added drop-wise in montanin wax, deresination montanin wax, peat wax or the deresination peat wax liquid of fusing; Contained coloring matter is oxidized to colorless substance in montanin wax, deresination montanin wax, peat wax or the deresination peat wax, after overcooling, filtration, obtains the smart wax and the decolouring oxidation waste liquid of light color.
In industrial production, adopting chromic acid to make the decolouring oxygenant, that montanin wax, deresination montanin wax, peat wax or deresination peat wax are carried out oxidative decoloration processing effect is better, and the decolouring oxidation waste liquid that this working method produced is a kind of chromium oxidation waste liquid that contains.
In containing chromium oxidation waste liquid, contain sexavalent chrome; Sexavalent chrome toxicity is extremely strong, and chromic toxicity exceeds more than 100 times than trivalent chromium, can not degrade at occurring in nature; Environment had persistent hazardness; Can and gather through digestive tube, respiratory tract, skin and mucous membrane intrusion human body, human body is caused chronic murder by poisoning, carcinogenic when serious.
Processing contains the traditional method of chromium oxidation waste liquid, is in containing chromium oxidation waste liquid, to throw in an amount of chemical reagent, will contain chromium oxidation waste liquid then and place for some time, wait sexavalent chrome to change into trivalent chromium after, be discharged in the physical environment.This method need consume a large amount of chemical reagent, and the treatment time is long, expense is high, and used chemical reagent also can cause secondary pollution to environment.
At present, membrane technique more and more receives publicity aspect wastewater treatment, the advantage that it has, and separation efficiency height, no phase transformation, non-secondary pollution, energy consumption are low, easy and simple to handle, separated product is easy to reclaim, level of automation is high.Membrane technique was not also met public reported at the treatment technology that montanin wax, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration contain chromium oxidation waste liquid.
Summary of the invention
The present invention is directed to montanin wax, deresination montanin wax, peat wax or deresination peat wax in the oxidative decoloration process; The chromium oxidation waste liquid that contains that produces lacks the recovery technology that is fit to; Directly discharging or during with the processing of traditional chemical reagent; There is the serious problem of environmental pollution, the separation and recovery method that contains chromium oxidation waste liquid that provides a kind of montanin wax, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration to produce, the technical scheme of this method may further comprise the steps:
(a) sulphur dioxide reduction: contained in the chromium oxidation waste liquid what montanin wax, deresination montanin wax, peat wax or the production of deresination peat wax oxidative decoloration produced; Control contains that chromium sulphate concentration is 40.5g/L in the chromium oxidation waste liquid; Sulfuric acid concentration is 543.3g/L; Hexavalent chromium concentration is 1-2g/L, in containing chromium oxidation waste liquid, feeds sulfur dioxide gas, and will contain the hexavalent chrome reduction that contains in the chromium oxidation waste liquid is trivalent chromium; The flow that the control sulfur dioxide gas feeds is 0.1-0.5kg/h; In temperature of reaction is that 20-50 ℃, stirring velocity are under the 100-500r/min condition, feeds to obtain containing chromium redox waste liquid after sulfurous gas finishes, and contains that chromic concentration is reduced to 5-10ug/L in the chromium redox waste liquid;
(b) waste liquid filters: will pass through the chromium redox waste liquid that contains that sulphur dioxide reduction obtains and filter with strainer; Said strainer is the oxidation resistant nuclepore membrane filter of anti-strong acid; The aperture of nuclepore membrane filter is 0.6-1.0um, and porosity is 50-80%, and the pressure during controlled filter is negative pressure 0.5-0.8MP; Remove the particulate state petroleum tailings, the chromium redox that contains that is not contained granule foreign is filtrated;
(c) diffusion dialysis separates: the chromium redox that contains that will obtain after will filtering is filtrated and is placed into the sour inlet of diffusion dialysis device; With sulfuric acid content is the water inlet that the sulphuric acid soln of 0-30g/L is put into the diffusion dialysis device; Containing between chromium redox filtrating and the said sulphuric acid soln in the diffusion dialysis device has homogeneous-phase anion exchange film to isolate; Left standstill 2-3 hour, static after, the flow velocity that control contains chromium redox filtrating is that the flow velocity of 350-550ml/h, said sulphuric acid soln is 400-600ml/h; Liquid outlet at the diffusion dialysis device reclaims the trivalent chromium redox flow at last; At water outlet reclaim(ed) sulfuric acid solution, liquid outlet obtains that chromic concentration is 35-45g/L in the trivalent chromium redox flow, and chromic rejection is 85-99%; Sulfuric acid concentration is 450-470g/L in the sulphuric acid soln that water outlet obtains, and the reclaim(ed) sulfuric acid rate reaches 80-88%L.
The diffusion dialysis device is a homogeneous-phase anion exchange film diffusion dialysis device in the technique scheme; Homogeneous-phase anion exchange film is a kind of in S203 or the DF120 homogeneous-phase anion exchange film.
The present invention uses the sulfur dioxide gas reduction of hexavalent chromium; Contain chromium oxidation waste liquid with what diffusive dialysis method separated that montanin wax, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration produce; Recovery obtains trivalent chromium redox flow and sulphuric acid soln, can carry out cycling and reutilization to two kinds of liquid; What oxidative decoloration produced contains chromium oxidation waste liquid through after the sulphur dioxide reduction; Containing of obtaining, chromic concentration was reduced to 5-10ug/L in the chromium redox waste liquid; Again after diffusion dialysis separates; Chromic concentration is 35-45g/L in the trivalent chromium redox flow that obtains, and chromic rejection is 85-99%; Vitriolic concentration is 450-470g/L in the sulphuric acid soln that recovery obtains, and the reclaim(ed) sulfuric acid rate reaches 80-88%.
The present invention does not introduce ionic impurity, no phase transformation, the non-secondary pollution beyond the system in reduction and sepn process, easy and simple to handle, equipment is simple; Efficient energy-saving; Environment is not discharged pollution-free, can realize the utilization again of resource, can effectively solve the pollution problem in chrome waste liquid field.
Description of drawings
Fig. 1 is a dynamic diffusion dialysis synoptic diagram of the present invention.
Specific embodiment
Embodiment 1:The separation and recovery method that contains chromium oxidation waste liquid that a kind of montanin wax, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration produce, the technical scheme of this method may further comprise the steps:
(a) sulphur dioxide reduction: get produce in montanin wax, deresination montanin wax, peat wax or the deresination peat wax oxidative decoloration course of processing contain chromium oxidation waste liquid 200L; Analysis and Control contains that chromium sulphate concentration is 40.5g/L in the chromium oxidation waste liquid; Sulfuric acid concentration is 543.3g/L, and hexavalent chromium concentration is 1g/L, in containing chromium oxidation waste liquid, feeds sulfur dioxide gas; To contain the hexavalent chrome reduction that contains in the chromium oxidation waste liquid is trivalent chromium; The flow that the control sulfur dioxide gas feeds is 0.1kg/h, is that 20 ℃, stirring velocity are under the 100r/min condition in temperature of reaction, and the time that feeds sulfur dioxide gas is 0.1h; Feed and to obtain containing chromium redox waste liquid after sulfurous gas finishes, containing of after the detection sulphur dioxide reduction, obtaining, chromic concentration was 10ug/L in the chromium redox waste liquid;
(b) waste liquid filters: will pass through the chromium redox waste liquid that contains that sulphur dioxide reduction obtains and filter with strainer; Said strainer is the oxidation resistant nuclepore membrane filter of anti-strong acid; The aperture of nuclepore membrane filter is 0.6um, and porosity is 50 %, and the pressure during controlled filter is negative pressure 1.0MP; Remove the particulate state petroleum tailings, the chromium redox that contains that is not contained granule foreign is filtrated;
(c) diffusion dialysis separates: as shown in Figure 1; Adopt homogeneous-phase anion exchange film diffusion dialysis device; The chromium redox filtrating that contains that obtains after filtering is placed in the waste liquid pool 2 of dynamic diffusion dialysis device; Water is placed in the pond 11 of dynamic diffusion dialysis device, homogeneous-phase anion exchange film 6 is DF120 homogeneous-phase anion exchange films, and the chromium redox filtrate water pump 5 that contains in the waste liquid pool 2 is pumped in the liquid bath 7 of diffusion dialysis device commuting case; Simultaneously the water in the pond 11 is pumped in the tank 10 of diffusion dialysis device commuting case with water pump 5, left standstill 2 hours; After leaving standstill, through valve on the liquid returning tube 13 and flow calorimeter 4, the flow velocity that control contains chromium redox filtrating is 400ml/h, and the flow velocity of water is 400ml/h, contains the SO in the chromium redox filtrating
4 2-Ion is diffused into the water of said tank 10 through homogeneous-phase anion exchange film 6 in the liquid bath of diffusion dialysis device commuting case 7, obtains the trivalent chromium redox flow at the liquid outlet of diffusion dialysis device, the sulphuric acid soln that obtains reclaiming at the water outlet of diffusion dialysis device;
After treatment, detect in the trivalent chromium redox flow that filtrate liquor pool 8 obtains Cr
3+Concentration be 37.73g/L, vitriolic concentration is 76.96 g/L; Detection in the reclaim(ed) sulfuric acid solution that outlet sump 9 obtains, Cr
3+Concentration be 1.32g/L, vitriolic concentration is 453.54g/L.
Embodiment 2:The separation and recovery method that contains chromium oxidation waste liquid that a kind of montanin wax, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration produce, the technical scheme of this method may further comprise the steps:
(a) sulphur dioxide reduction: get produce in montanin wax, deresination montanin wax, peat wax or the deresination peat wax oxidative decoloration course of processing contain chromium oxidation waste liquid 200L; Analysis and Control contains that chromium sulphate concentration is 40.5g/L in the chromium oxidation waste liquid; Sulfuric acid concentration is 543.3g/L, and hexavalent chromium concentration is 1.5g/L, in containing chromium oxidation waste liquid, feeds sulfur dioxide gas; To contain the hexavalent chrome reduction that contains in the chromium oxidation waste liquid is trivalent chromium; The flow that the control sulfur dioxide gas feeds is 0.1kg/h, is that 30 ℃, stirring velocity are under the 200r/min condition in temperature of reaction, and the time that feeds sulfur dioxide gas is 0.1h; Feed and to obtain containing chromium redox waste liquid after sulfurous gas finishes, containing of after the detection sulphur dioxide reduction, obtaining, chromic concentration was 8ug/L in the chromium redox waste liquid;
(b) waste liquid filters: will pass through the chromium redox waste liquid that contains that sulphur dioxide reduction obtains and filter with strainer; Said strainer is the oxidation resistant nuclepore membrane filter of anti-strong acid; The aperture of nuclepore membrane filter is 0.8um, and porosity is 60 %, and the pressure during controlled filter is negative pressure 0.8MP; Remove the particulate state petroleum tailings, the chromium redox that contains that is not contained granule foreign is filtrated;
(c) diffusion dialysis separates: as shown in Figure 1; Adopt homogeneous-phase anion exchange film diffusion dialysis device; The chromium redox filtrating that contains that obtains after filtering is placed in the waste liquid pool 1 of dynamic diffusion dialysis device; With sulfuric acid content is that the sulphuric acid soln of 10g/L is placed in the pond 11 of dynamic diffusion dialysis device, and homogeneous-phase anion exchange film 6 is DF120 homogeneous-phase anion exchange films, and the chromium redox filtrate water pump 5 that contains in the waste liquid pool 2 is pumped in the liquid bath 7 of diffusion dialysis device commuting case; Simultaneously the sulphuric acid soln in the pond 11 is pumped in the tank 10 of diffusion dialysis device commuting case with water pump 5, left standstill 2.5 hours; After leaving standstill, through valve on the liquid returning tube 13 and flow calorimeter 4, the flow velocity that control contains chromium redox filtrating is 400ml/h, and the flow velocity of sulphuric acid soln is 400ml/h, contains the SO in the chromium redox filtrating
4 2-Ion is diffused into the sulphuric acid soln of said tank 10 through homogeneous-phase anion exchange film 6 in the liquid bath 7 of diffusion dialysis device commuting case; Liquid outlet at the diffusion dialysis device obtains the trivalent chromium redox flow, the sulphuric acid soln that obtains reclaiming at the water outlet of diffusion dialysis device;
After treatment, detect in the trivalent chromium redox flow that filtrate liquor pool 8 obtains Cr
3+Concentration be 38.11g/L, vitriolic concentration is 65.67 g/L; Detection in the reclaim(ed) sulfuric acid solution that outlet sump 9 obtains, Cr
3+Concentration be 1.53g/L, vitriolic concentration is 465.68g/L.
Embodiment 3:The separation and recovery method that contains chromium oxidation waste liquid that a kind of montanin wax, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration produce, the technical scheme of this method may further comprise the steps:
(a) sulphur dioxide reduction: get produce in montanin wax, deresination montanin wax, peat wax or the deresination peat wax oxidative decoloration course of processing contain chromium oxidation waste liquid 200L; Analysis and Control contains that chromium sulphate concentration is 40.5g/L in the chromium oxidation waste liquid; Sulfuric acid concentration is 543.3g/L, and hexavalent chromium concentration is 2.0g/L, in containing chromium oxidation waste liquid, feeds sulfur dioxide gas; To contain the hexavalent chrome reduction that contains in the chromium oxidation waste liquid is trivalent chromium; The flow that the control sulfur dioxide gas feeds is 0.1kg/h, is that 40 ℃, stirring velocity are under the 300r/min condition in temperature of reaction, and the time that feeds sulfur dioxide gas is 0.1h; Feed and to obtain containing chromium redox waste liquid after sulfurous gas finishes, containing of after the detection sulphur dioxide reduction, obtaining, chromic concentration was 5ug/L in the chromium redox waste liquid;
(b) waste liquid filters: will pass through the chromium redox waste liquid that contains that sulphur dioxide reduction obtains and filter with strainer; Said strainer is the oxidation resistant nuclepore membrane filter of anti-strong acid; The aperture of nuclepore membrane filter is 1.0um, and porosity is 70 %, and the pressure during controlled filter is negative pressure 0.6MP; Remove the particulate state petroleum tailings, the chromium redox that contains that is not contained granule foreign is filtrated;
(c) diffusion dialysis separates: as shown in Figure 1; Adopt homogeneous-phase anion exchange film diffusion dialysis device; The chromium redox filtrating that contains that obtains after filtering is placed in the waste liquid pool 2 of dynamic diffusion dialysis device; With sulfuric acid content is that the sulphuric acid soln of 30g/L is placed in the pond 11 of dynamic diffusion dialysis device, and homogeneous-phase anion exchange film 6 is DF120 homogeneous-phase anion exchange films, and the chromium redox filtrate water pump 5 that contains in the waste liquid pool 2 is pumped in the liquid bath 7 of diffusion dialysis device commuting case; Simultaneously the sulphuric acid soln in the pond 11 is pumped in the tank 10 of diffusion dialysis device commuting case with water pump 5, left standstill 3 hours; After leaving standstill, through valve on the liquid returning tube 13 and flow calorimeter 4, the flow velocity that control contains chromium redox filtrating is 500ml/h, and the flow velocity of sulphuric acid soln is 500ml/h, contains the SO in the chromium redox filtrating
4 2-Ion is diffused into the sulphuric acid soln of said tank 10 through homogeneous-phase anion exchange film 6 in the liquid bath 7 of diffusion dialysis device commuting case; Liquid outlet at the diffusion dialysis device obtains the trivalent chromium redox flow, the sulphuric acid soln that obtains reclaiming at the water outlet of diffusion dialysis device;
After treatment, detect in the trivalent chromium redox flow that filtrate liquor pool 8 obtains Cr
3+Concentration be 38.91g/L, vitriolic concentration is 70.22 g/L; Detection in the reclaim(ed) sulfuric acid solution that outlet sump 9 obtains, Cr
3+Concentration be 1.13g/L, vitriolic concentration is 469.76g/L.
Claims (4)
1. the separation and recovery method that contains chromium oxidation waste liquid of montanin wax, deresination montanin wax, peat wax or the generation of deresination peat wax oxidative decoloration is characterized in that, may further comprise the steps:
(a) sulphur dioxide reduction: contained in the chromium oxidation waste liquid what montanin wax, deresination montanin wax, peat wax or the production of deresination peat wax oxidative decoloration produced; Control contains that chromium sulphate concentration is 40.5g/L in the chromium oxidation waste liquid; Sulfuric acid concentration is 543.3g/L, and hexavalent chromium concentration is 1-2g/L, in containing chromium oxidation waste liquid, feeds sulfur dioxide gas; The flow that the control sulfur dioxide gas feeds is 0.1-0.5kg/h; In temperature of reaction is that 20-50 ℃, stirring velocity are under the 100-500r/min condition, feeds to obtain containing chromium redox waste liquid after sulfurous gas finishes, and contains that chromic concentration is reduced to 5-10ug/L in the chromium redox waste liquid;
(b) waste liquid filters: will pass through the chromium redox waste liquid that contains that sulphur dioxide reduction obtains and filter with strainer; Pore size filter is 0.6-1.0 um; Porosity is 50-80%; Pressure during controlled filter is negative pressure 0.5-0.8MP, removes the particulate state petroleum tailings, and the chromium redox that contains that is not contained granule foreign is filtrated;
(c) diffusion dialysis separates: the chromium redox that contains that will obtain after will filtering is filtrated and is placed into the sour inlet of diffusion dialysis device; With sulfuric acid content is the water inlet that the sulphuric acid soln of 0-30g/L is put into the diffusion dialysis device; Containing between chromium redox filtrating and the said sulphuric acid soln in the diffusion dialysis device has homogeneous-phase anion exchange film to isolate; Left standstill 2-3 hour, static after, the flow velocity that control contains chromium redox filtrating is that the flow velocity of 350-550ml/h, said sulphuric acid soln is 400-600ml/h; Liquid outlet at the diffusion dialysis device reclaims the trivalent chromium redox flow at last; At water outlet reclaim(ed) sulfuric acid solution, liquid outlet obtains that chromic concentration is 35-45g/L in the trivalent chromium redox flow, and chromic rejection is 85-99%; Sulfuric acid concentration is 450-470g/L in the sulphuric acid soln that water outlet obtains, and the reclaim(ed) sulfuric acid rate reaches 80-88%L.
2. the separation and recovery method that contains chromium oxidation waste liquid that montanin wax as claimed in claim 1, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration produce, it is characterized in that: said strainer is the oxidation resistant nuclepore membrane filter of anti-strong acid.
3. the separation and recovery method that contains chromium oxidation waste liquid that montanin wax as claimed in claim 1, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration produce, it is characterized in that: said diffusion dialysis device is a homogeneous-phase anion exchange film diffusion dialysis device.
4. the separation and recovery method that contains chromium oxidation waste liquid that montanin wax as claimed in claim 3, deresination montanin wax, peat wax or deresination peat wax oxidative decoloration produce is characterized in that: homogeneous-phase anion exchange film is a kind of in S203 or the DF120 homogeneous-phase anion exchange film.
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| CN201210294525.1A CN102815821B (en) | 2012-08-20 | 2012-08-20 | Method for separating and recycling chrome-contained oxide waste liquid produced by oxidation and decoloration of lignite wax, deresination lignite wax, peat wax or deresination peat wax |
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|---|---|---|---|
| CN201210294525.1A CN102815821B (en) | 2012-08-20 | 2012-08-20 | Method for separating and recycling chrome-contained oxide waste liquid produced by oxidation and decoloration of lignite wax, deresination lignite wax, peat wax or deresination peat wax |
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| CN102815821A true CN102815821A (en) | 2012-12-12 |
| CN102815821B CN102815821B (en) | 2014-01-01 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106222690A (en) * | 2016-08-24 | 2016-12-14 | 神华国能宝清煤电化有限公司 | A kind of three film four Room aqueous solution plate and frame electrolysis bath and application thereof |
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| CN103130280A (en) * | 2013-03-25 | 2013-06-05 | 国药集团化学试剂有限公司 | Method for improving quality of industrial chromic chloride |
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| CN106222690A (en) * | 2016-08-24 | 2016-12-14 | 神华国能宝清煤电化有限公司 | A kind of three film four Room aqueous solution plate and frame electrolysis bath and application thereof |
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|---|---|
| CN102815821B (en) | 2014-01-01 |
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