CN211896157U - Nitric acid wastewater treatment system containing aluminum nitrate - Google Patents
Nitric acid wastewater treatment system containing aluminum nitrate Download PDFInfo
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- CN211896157U CN211896157U CN202020219677.5U CN202020219677U CN211896157U CN 211896157 U CN211896157 U CN 211896157U CN 202020219677 U CN202020219677 U CN 202020219677U CN 211896157 U CN211896157 U CN 211896157U
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- falling film
- aluminum sulfate
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- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 title claims abstract description 125
- 229910017604 nitric acid Inorganic materials 0.000 title claims abstract description 124
- BNGXYYYYKUGPPF-UHFFFAOYSA-M (3-methylphenyl)methyl-triphenylphosphanium;chloride Chemical compound [Cl-].CC1=CC=CC(C[P+](C=2C=CC=CC=2)(C=2C=CC=CC=2)C=2C=CC=CC=2)=C1 BNGXYYYYKUGPPF-UHFFFAOYSA-M 0.000 title claims abstract description 60
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 16
- 239000011552 falling film Substances 0.000 claims abstract description 180
- 238000001704 evaporation Methods 0.000 claims abstract description 85
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims abstract description 83
- 230000008020 evaporation Effects 0.000 claims abstract description 81
- 239000002351 wastewater Substances 0.000 claims abstract description 37
- 238000002425 crystallisation Methods 0.000 claims abstract description 22
- 230000008025 crystallization Effects 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 15
- 238000001816 cooling Methods 0.000 claims abstract description 14
- 238000000746 purification Methods 0.000 claims abstract description 11
- 238000012546 transfer Methods 0.000 claims abstract description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 179
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 97
- 239000011347 resin Substances 0.000 claims description 76
- 229920005989 resin Polymers 0.000 claims description 76
- 239000007788 liquid Substances 0.000 claims description 31
- 238000004140 cleaning Methods 0.000 claims description 30
- 229910052782 aluminium Inorganic materials 0.000 claims description 28
- -1 aluminum ions Chemical class 0.000 claims description 18
- 239000002699 waste material Substances 0.000 claims description 13
- 238000004064 recycling Methods 0.000 claims description 8
- JLDSOYXADOWAKB-UHFFFAOYSA-N aluminium nitrate Chemical compound [Al+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O JLDSOYXADOWAKB-UHFFFAOYSA-N 0.000 claims description 6
- 230000009290 primary effect Effects 0.000 claims description 6
- 238000003795 desorption Methods 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 4
- 238000007790 scraping Methods 0.000 claims description 3
- 238000011085 pressure filtration Methods 0.000 claims description 2
- 238000010992 reflux Methods 0.000 claims description 2
- 235000011128 aluminium sulphate Nutrition 0.000 abstract description 10
- 229910000329 aluminium sulfate Inorganic materials 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 2
- 230000002349 favourable effect Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 54
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical group [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 10
- 238000005406 washing Methods 0.000 description 10
- 239000010410 layer Substances 0.000 description 9
- 239000001117 sulphuric acid Substances 0.000 description 9
- 235000011149 sulphuric acid Nutrition 0.000 description 9
- 238000004458 analytical method Methods 0.000 description 8
- 238000013461 design Methods 0.000 description 7
- 238000005086 pumping Methods 0.000 description 7
- 238000007599 discharging Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 239000002609 medium Substances 0.000 description 6
- 239000000498 cooling water Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 238000001035 drying Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000012452 mother liquor Substances 0.000 description 5
- 229920006395 saturated elastomer Polymers 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 239000013078 crystal Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000012047 saturated solution Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 239000011229 interlayer Substances 0.000 description 2
- 238000005304 joining Methods 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- AMVQGJHFDJVOOB-UHFFFAOYSA-H aluminium sulfate octadecahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.[Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O AMVQGJHFDJVOOB-UHFFFAOYSA-H 0.000 description 1
- 239000001164 aluminium sulphate Substances 0.000 description 1
- REDXJYDRNCIFBQ-UHFFFAOYSA-N aluminium(3+) Chemical compound [Al+3] REDXJYDRNCIFBQ-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- BUACSMWVFUNQET-UHFFFAOYSA-H dialuminum;trisulfate;hydrate Chemical compound O.[Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O BUACSMWVFUNQET-UHFFFAOYSA-H 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000011888 foil Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 239000001963 growth medium Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
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Abstract
The utility model discloses a nitric acid wastewater treatment system containing aluminum nitrate, which comprises a two-stage column-passing separation system and an aluminum sulfate purification system, wherein the aluminum sulfate purification system comprises an aluminum sulfate feeding tank, a preheater, a double-effect three-stage falling-film evaporator, a cooling crystallization tank, a crystallization transfer tank, a filter press, a high-level tank and a scraper, which are connected in sequence, wherein the double-effect three-stage falling-film evaporator is used for evaporating and concentrating aluminum sulfate solution for multiple times; the aluminum sulfate feeding tank is connected with the aluminum sulfate solution tank. The method for treating the nitric acid wastewater containing the aluminum nitrate based on the wastewater treatment system has small evaporation amount and low production risk; the replacement is thorough, the nitric acid content in the obtained aluminum sulfate solution is less, and aluminum sulfate better than the national standard can be further produced; the utility model discloses the technology is more energy-conserving, and the aluminium sulfate product quality that obtains is higher, and whole temperature is not too high again, is favorable to long-time steady operation.
Description
Technical Field
The utility model relates to a spent acid treatment technical field especially relates to a nitric acid effluent disposal system who contains aluminum nitrate.
Background
The corrosion procedure in the electrode foil production process needs a large amount of mixed acid, so a large amount of strong acid-containing wastewater is generated, one of the main wastewater is aluminum-containing nitric acid wastewater, the general treatment method is to directly neutralize and discharge the aluminum-containing nitric acid wastewater, and although the acidity can be greatly reduced, a large amount of NO exists in the aluminum-containing nitric acid wastewater3 -、Al3+Still exist in an ionic state, can cause total nitrogen, serious standard exceeding and resource waste, and does not meet the requirement of environmental protection. Chinese patent document (application No. 201711286050.0) discloses a method for treating wastewater containing aluminum and nitric acid, which comprises the following steps: carrying out multi-effect evaporation treatment on the aluminum-containing nitric acid wastewater to obtain a concentrated solution; cooling and crystallizing the concentrated solution to obtain a crystalline liquid; carrying out solid-liquid separation on the crystallization liquid to obtain filtrate and crystal aluminum nitrate; recycling the filtrate, dissolving the crystal aluminum nitrate, and adding sulfuric acid for replacement treatment to obtain nitric acid and aluminum sulfate; in the cooling crystallization treatment process, 10-11 mol/L nitric acid is added into the concentrated solution, and the volume ratio of the added nitric acid to the concentrated solution is (1.3-1.5): 1.
However, the prior art has the following disadvantages:
the evaporation amount is large, the hydrated aluminum nitrate is decomposed at 135 degrees, triple effect evaporation is adopted, and because the solubility of the aluminum nitrate is greatly changed along with the temperature, the final effect temperature cannot be too low, the first effect temperature is higher, and the production risk is higher;
sulfuric acid is added into the separated aluminum nitrate, so that the aluminum nitrate can be replaced, but the replacement is incomplete, the obtained aluminum sulfate contains more nitric acid, and the residual sulfuric acid is not treated, so that the waste of the nitric acid and the impurity of the aluminum sulfate are caused.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to overcome the deficiencies in the prior art and provide a nitric acid wastewater treatment system containing aluminum nitrate and a treatment method thereof.
The utility model provides a technical scheme that its technical problem adopted is:
a nitric acid wastewater treatment system containing aluminum nitrate comprises:
the two-stage column-passing separation system is used for separating out aluminum ions in the nitric acid wastewater containing aluminum nitrate and comprises at least 3 resin columns and serial pipelines with the same number as the resin columns, an upper serial connection port, a feed inlet, a compressed air inlet, a cleaning water inlet and a sulfuric acid inlet are arranged at the top ends of the resin columns in parallel, and a lower serial connection port, an aluminum sulfate solution outlet, a nitric acid waste liquid outlet and a nitric acid wastewater outlet containing aluminum nitrate are arranged at the bottom ends of the resin columns in parallel; the resin columns are sequentially connected in series through the series pipelines connected between the lower series connection interface and the upper series connection interface to form a loop;
the aluminum nitrate tank is provided with a liquid outlet connected with the feed inlet and is used for introducing pretreated nitric acid wastewater containing aluminum nitrate into the resin column; the aluminum nitrate tank is also provided with a liquid return port connected with the nitric acid wastewater outlet containing aluminum nitrate and used for receiving the saturated nitric acid wastewater containing aluminum nitrate in the resin column;
a compressed air line connected to the compressed air inlet for introducing compressed air into the resin column; a cleaning water tank connected with the cleaning water inlet and used for providing cleaning water for the resin column, and a sulfuric acid tank connected with the sulfuric acid inlet and used for providing a sulfuric acid solution for desorbing aluminum ions for the resin column; the aluminum sulfate solution tank is connected with the aluminum sulfate solution outlet and is used for receiving the aluminum sulfate solution discharged from the resin column; the recycling nitric acid tank is connected with the nitric acid waste liquid outlet and is used for receiving the nitric acid waste liquid discharged after the aluminum adsorption is carried out by the two-stage column separation system;
the system comprises an aluminum sulfate feeding tank, a preheater, a double-effect three-stage falling-film evaporator for evaporating and concentrating aluminum sulfate solution for multiple times, a cooling crystallization tank, a crystallization transfer tank, a pressure filter, a high-level tank for receiving the solid after pressure filtration and a scraping machine which are connected in sequence; the aluminum sulfate feeding tank is connected with the aluminum sulfate solution tank.
Further, there are 4 resin columns, be A post, B post, C post and D post respectively, the series line has 4, be the A series line that is used for connecting the lower series connection interface of A post and the last series connection mouth of B post respectively, be used for the lower series connection interface of B post and the last series connection mouth of C post be connected B series line, be used for the lower series connection interface of C post and the last series connection mouth of D post be connected C series line to and be used for the lower series connection interface of D post and the last series connection mouth of A post be connected D series line.
The device further comprises a recycling nitric acid tank connected with the nitric acid waste liquid outlet, a dilute nitric acid outlet is further connected to the lower end of the resin column in parallel, and the dilute nitric acid outlet is connected with a dilute nitric acid tank and used for receiving dilute nitric acid discharged by water replacement before aluminum ion desorption in the resin column; the dilute nitric acid tank is also connected with the cleaning water inlet of the resin column and is used for introducing dilute nitric acid into the resin column for replacement. The dilute nitric acid is used for replacing, so that the consumption of washing water is reduced, the nitric acid content in the dilute nitric acid is improved, the dilute nitric acid is used for preparing nitric acid, the loss of the nitric acid is reduced, if the dilute nitric acid is directly replaced by water, the concentration of the nitric acid in the washing water is too low, the generated washing water is too much, the previous preparation of the nitric acid does not use so much water, and the waste of the nitric acid is also caused.
Further, the lower end of the resin column is also provided with a dilute sulfuric acid outlet in parallel, and the dilute sulfuric acid outlet is connected with a dilute sulfuric acid tank and used for receiving dilute sulfuric acid discharged by water replacement after aluminum ions are desorbed in the resin column; the dilute sulfuric acid tank is connected with the cleaning water inlet of the resin column and used for introducing dilute sulfuric acid into the resin column for replacement, and the dilute sulfuric acid is still placed into the dilute sulfuric acid tank after replacement.
Furthermore, the bottom of the resin column is connected in parallel with a sulfuric acid outlet, and the sulfuric acid outlet is connected with a sulfuric acid tank. When the aluminum ion analysis in the resin column is nearly complete (when the aluminum ion concentration detected at the outlet of the aluminum sulfate solution is nearly 0), the sulfuric acid is basically in the resin column, and the sulfuric acid is discharged to a sulfuric acid tank through a sulfuric acid outlet and used for next analysis.
Further, the two-effect three-stage falling-film evaporator comprises:
the first-effect falling film evaporator is used for carrying out first-effect falling film evaporation on the aluminum sulfate solution preheated by the preheater to form first-effect concentrated solution;
the double-effect falling film evaporator is used for carrying out double-effect falling film evaporation on the primary-effect concentrated solution from the primary-effect falling film evaporator to form a double-effect concentrated solution;
the three-level falling film evaporator is used for carrying out triple-effect falling film evaporation on the double-effect concentrated solution from the double-effect falling film evaporator to form triple-effect concentrated solution;
the first-effect falling-film evaporator is provided with a first-effect secondary steam outlet, the first-effect secondary steam outlet is connected with the second-effect falling-film evaporator through a pipeline and is used for sending secondary steam generated by the first-effect falling-film evaporator into the second-effect falling-film evaporator to be used as a heat exchange medium of the second-effect falling-film evaporator; the evaporator further comprises a steam pipeline, wherein the steam pipeline is respectively connected with the steam inlets of the first-effect falling-film evaporator and the third-level falling-film evaporator and is used as a heat exchange medium of the first-effect falling-film evaporator and the third-level falling-film evaporator.
Specifically, the first-effect falling film evaporator comprises a first-effect falling film heat exchanger, a first-effect circulating pipeline, a first-effect circulating pump and a first-effect falling film evaporation chamber, the preheater is communicated with the top end of a tube pass of the first-effect falling film heat exchanger through a pipeline, the bottom end of the tube pass of the first-effect falling film heat exchanger is communicated with the lower end of the first-effect falling film evaporation chamber, the upper end of the tube pass of the first-effect falling film heat exchanger is communicated with the bottom end of the first-effect falling film evaporation chamber through a second-effect circulating pipeline, and the top end of the first-effect falling film evaporation chamber is provided with the first-effect secondary steam outlet;
the double-effect falling film evaporator comprises a double-effect falling film heat exchanger, a double-effect circulating pipeline, a double-effect circulating pump and a double-effect falling film evaporation chamber, wherein the double-effect circulating pump and the double-effect falling film evaporation chamber are arranged on the double-effect circulating pipeline;
the three-stage falling film evaporator comprises a triple-effect falling film heat exchanger, a triple-effect circulating pipeline, a triple-effect circulating pump and a triple-effect falling film evaporation chamber, wherein the triple-effect circulating pump and the triple-effect falling film evaporation chamber are arranged on the triple-effect circulating pipeline, the lower end of the triple-effect falling film evaporation chamber is communicated with the bottom end of a tube pass of the triple-effect falling film heat exchanger, the upper end of the tube pass of the triple-effect falling film heat exchanger is communicated with the bottom end of the triple-effect falling film evaporation chamber through the triple-effect circulating pipeline, the lower end of the double-effect falling film evaporation chamber is communicated with the upper end of the tube pass of the triple-effect falling film heat exchanger, and a.
More specifically, the aluminum sulfate purification system further comprises a first condensate water tank and a second condensate water tank, wherein the first condensate water tank is used for receiving secondary steam generated by the double-effect falling film evaporation chamber and the triple-effect falling film evaporation chamber and condensate water generated in a shell layer of the double-effect falling film heat exchanger, and the second condensate water tank is used for receiving condensate water generated in a shell layer of the single-effect falling film heat exchanger and a shell layer of the triple-effect falling film heat exchanger.
Further, the second condensate water tank is connected with the preheater and is used for introducing condensate water into the preheater as a heat exchange medium of the aluminum sulfate solution.
In order to maintain the normal pressure state of the high-pressure pipe and avoid overpressure, the high-pressure pipe preferably further comprises a first heat exchanger, wherein a tube side inlet and a tube side outlet of the first heat exchanger are both connected with the high-level tank and used for condensing and refluxing hot steam generated by the high-level tank.
The utility model has the advantages that: the system for treating the nitric acid wastewater containing the aluminum nitrate and the method for treating the nitric acid wastewater containing the aluminum nitrate based on the system have the advantages of small evaporation capacity and low production risk; the replacement is thorough, and the content of nitric acid in the obtained aluminum sulfate solution is less; the utility model discloses with the aluminium separation back, can resolve well with 20 ~ 30% sulphuric acid resolution (20-30% sulphuric acid, and the solubility of aluminium sulfate is minimum when finally concentrating to 55-60%, be convenient for fully take out the aluminium sulfate, the volume that needs the evaporation is still little, sulphuric acid concentration again highly can destroy the resin) after will contain sulphuric acid aluminium sulfate concentration, reach 55% -60% at sulphuric acid content, aluminium sulfate is the lowest in 55% -60% sulphuric acid, as long as 2-3 times the concentration of analytic sulphuric acid, through the crystal separation, will remain a small amount of sulphuric acid reaction again, can produce the aluminium sulfate that is superior to national standard; the utility model discloses technology is more energy-conserving, and whole temperature is not too high again, is favorable to long-time steady operation.
Drawings
The present invention will be further explained with reference to the drawings and examples.
FIG. 1 is a schematic diagram of a device for obtaining aluminum sulfate by column separation in a nitric acid wastewater treatment system containing aluminum nitrate.
Fig. 2 is a schematic diagram of the two-stage column separation system of fig. 1.
FIG. 3 is a schematic diagram of an aluminum sulfate purification system in the nitric acid wastewater treatment system containing aluminum nitrate.
Fig. 4 is a schematic diagram of the crystal purification system of fig. 3.
Fig. 5 is a schematic diagram of the falling film evaporation system of fig. 3.
The reference numbers in the figures are: 1. sulfuric acid tank, 2 sulfuric acid pump, 3 cleaning water tank, 4 cleaning water pump, 5 aluminium nitrate tank, 6 aluminium nitrate pump, 7 recycling nitric acid tank, 8 recycling nitric acid pump, 9 dilute nitric acid tank, 10 dilute nitric acid pump, 11 dilute sulfuric acid tank, 12 dilute sulfuric acid pump, 13 aluminium sulfate solution tank, 14 aluminium sulfate raw material pump, 15 second sulfuric acid tank, 16 condensing water pump, 17V-09 tank, 18 aluminium sulfate feeding tank, 19 feeding pump, 20 first mother liquor pump, 21 elevated tank E, 22 elevated tank A/B, 23 elevated tank C/D, 24 second mother liquor pump, 25 crystallization transfer tank, 26 scraper, 27 first filter press, 28 second filter press, 29 first heat exchanger, 30 first cooling crystallization tank, 31 second cooling crystallization tank, 32 preheater, 33 one-effect falling film heat exchanger, 34. The system comprises a first-effect falling film evaporation chamber, a second-effect falling film heat exchanger, a 36-effect falling film evaporation chamber, a 37-effect falling film heat exchanger, a 38-effect falling film evaporation chamber, a 39-effect second heat exchanger, a 40-effect circulating pump, a 41-effect condensation water tank, a 42-effect circulating pump, a 43-effect circulating pump, a 44-effect condensation water tank, a 45-vacuum pump, a 46-effect third heat exchanger and a 47-01 condensation water tank;
Q1: a two-stage column-passing separation system;
Q2: a crystallization purification system;
Q3: falling film evaporation systems.
Detailed Description
The present invention will now be described in further detail with reference to the accompanying drawings. The drawings are simplified schematic drawings, which illustrate the basic structure of the invention only in a schematic way, and thus show only the components that are relevant to the invention, and the directions and references (e.g., upper, lower, left, right, etc.) may be used only to help describe the features in the drawings. The following detailed description is, therefore, not to be taken in a limiting sense, and the scope of the claimed subject matter is defined only by the appended claims and equivalents thereof.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted", "connected", "disposed" and "provided" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations. Unless otherwise specifically stated or limited, the terms "pipe", "line" and "pipeline" are to be understood in a broad sense, e.g. they may be pipes alone or in combination with control valves and/or flow meters and/or thermometers and/or pumps, which may be disposed on the pipes as required, and the specific meaning of the terms in the present invention may be understood by those skilled in the art from the specific context.
Referring to fig. 1 to 4 (the direction of arrows in the figures is the direction of fluid flow), a nitric acid wastewater treatment system containing aluminum nitrate comprises a two-stage column-passing separation system, an aluminum nitrate tank, a compressed air pipeline, a cleaning water tank, a sulfuric acid tank, an aluminum sulfate solution tank and an aluminum sulfate purification system.
The two-stage column-passing separation system is used for separating aluminum ions from the nitric acid wastewater containing aluminum nitrate, and comprises at least 3 resin columns and serial pipelines with the same number as the resin columns (the column-passing efficiency can be reduced when the resin columns are not connected in series or are connected in series). The top end of the resin column is provided with an upper serial interface, a feed inlet, a compressed air inlet, a cleaning water inlet and a sulfuric acid inlet in parallel, and the bottom end of the resin column is provided with a lower serial interface, an aluminum sulfate solution outlet, a nitric acid waste liquid outlet and a nitric acid waste water outlet containing aluminum nitrate in parallel; the resin columns are sequentially connected in series through the series pipelines connected between the lower series interface and the upper series interface to form a loop.
The specific number of the resin columns and the series pipelines can be adjusted according to the actual engineering requirements, and the resin columns and the series pipelines of the embodiment have 4, specifically: the number of the resin columns is 4, the resin columns are respectively an A column, a B column, a C column and a D column, the number of the series pipelines is 4, and the series pipelines are respectively an A series pipeline for connecting a lower series interface of the A column with an upper series connecting port of the B column, a B series pipeline for connecting a lower series interface of the B column with an upper series connecting port of the C column, a C series pipeline for connecting a lower series interface of the C column with an upper series connecting port of the D column, and a D series pipeline for connecting a lower series interface of the D column with an upper series connecting port of the A column.
The aluminum nitrate groove is provided with a liquid outlet connected with the feed inlet, and is specifically connected with the resin column through a pipeline provided with aluminum nitrate pumps PP-103A and B for introducing pretreated nitric acid wastewater containing aluminum nitrate into the resin column. The aluminum nitrate tank is also provided with a liquid return port connected with a nitric acid waste water outlet containing aluminum nitrate and used for receiving the nitric acid waste water containing aluminum nitrate after the resin column is saturated.
The compressed air line is connected with a compressed air inlet of the resin column and is used for introducing compressed air into the resin column. The washing water tank is connected to a washing water inlet of the resin column for supplying washing water into the resin column. The sulfuric acid tank is connected with a sulfuric acid inlet of the resin column and is used for providing a sulfuric acid solution for aluminum ion desorption into the resin column. The aluminum sulfate solution tank is connected with an aluminum sulfate solution outlet of the resin column and is used for receiving the aluminum sulfate solution discharged from the resin column.
The device also comprises a recycling nitric acid tank connected with a nitric acid waste liquid outlet of the resin column, wherein a dilute nitric acid outlet is further connected to the lower end of the resin column in parallel, and the dilute nitric acid outlet is connected with a dilute nitric acid tank and used for receiving dilute nitric acid discharged by water replacement before aluminum ion desorption in the resin column. And the dilute nitric acid tank is also connected with the cleaning water inlet of the resin column and is used for introducing dilute nitric acid into the resin column for replacement. The purpose that so sets up is convenient for earlier replace with dilute nitric acid among the cleaning process before the analytic aluminium ion of sulphuric acid, and the purpose of replacing with dilute nitric acid is to reduce the washing water quantity, improves nitric acid content in the dilute nitric acid, and the back is used for joining in marriage the nitric acid, reduces the loss of nitric acid, if direct water replacement, the nitric acid concentration in the washing water is too low, and the washing water yield that produces is too much moreover, and preceding joining in marriage the nitric acid and can't use so much water, also leads to the waste of nitric acid. And placing the diluted nitric acid into a diluted nitric acid tank after the diluted nitric acid is replaced. Furthermore, the lower end of the resin column is also provided with a dilute sulfuric acid outlet in parallel, and the dilute sulfuric acid outlet is connected with a dilute sulfuric acid tank and used for receiving dilute sulfuric acid discharged by water replacement after aluminum ion desorption in the resin column. And the dilute sulfuric acid tank is connected with the cleaning water inlet of the resin column and is used for introducing dilute sulfuric acid into the resin column for replacement. The purpose of the arrangement is that dilute sulfuric acid is convenient to replace in the cleaning process after aluminum ions are resolved by sulfuric acid, the purpose of replacing with dilute sulfuric acid is to reduce the amount of washing water, improve the sulfuric acid content in dilute sulfuric acid, and then the dilute sulfuric acid is used for preparing sulfuric acid for resolution, so that the loss of sulfuric acid is reduced. And (4) placing the diluted nitric acid into a diluted sulfuric acid tank after the diluted nitric acid is replaced. The bottom of the resin column is connected in parallel with a sulfuric acid outlet, and the sulfuric acid outlet is connected with a sulfuric acid tank. When the aluminum ion analysis in the resin column is nearly complete (when the aluminum ion concentration detected at the outlet of the aluminum sulfate solution is nearly 0), the sulfuric acid is basically in the resin column, and the sulfuric acid is discharged to a sulfuric acid tank through a sulfuric acid outlet and used for next analysis.
The aluminum sulfate purification system comprises an aluminum sulfate feeding tank 18 and a falling film evaporation system Q which are sequentially connected along the aluminum sulfate advancing direction3And a crystallization purification system Q2. Crystallization purification system Q2Comprises a cooling crystallization tank (the cooling crystallization tank comprises a first cooling crystallization tank 30 and a second cooling crystallization tank 31 in the embodiment), a crystallization transfer tank 25, a second mother liquor pump 24 and a filter press (the embodiment is that the filter press is a solid product)The example filter press includes a first filter press 26 and a second filter press 27), a head tank for receiving filter-pressed solids, a first mother liquor pump 20, and a scraper 26; the aluminum sulfate feeding tank 18 is connected with the aluminum sulfate solution tank 13, and during operation, the aluminum sulfate solution in the aluminum sulfate solution tank 13 is pumped to the aluminum sulfate feeding tank 18 through the aluminum sulfate raw material pump 14.
Falling film evaporation system Q3Comprises a preheater 32 and a two-effect three-stage falling-film evaporator, wherein the preheater 32 and the two-effect three-stage falling-film evaporator are sequentially connected along the advancing direction of aluminum sulfate.
Specifically, the two-effect three-stage falling-film evaporator comprises:
the first-effect falling film evaporator is used for carrying out first-effect falling film evaporation on the aluminum sulfate solution preheated by the preheater to form first-effect concentrated solution;
the double-effect falling film evaporator is used for carrying out double-effect falling film evaporation on the primary-effect concentrated solution from the primary-effect falling film evaporator to form a double-effect concentrated solution;
the three-level falling film evaporator is used for carrying out triple-effect falling film evaporation on the double-effect concentrated solution from the double-effect falling film evaporator to form triple-effect concentrated solution;
the first-effect falling-film evaporator is provided with a first-effect secondary steam outlet, the first-effect secondary steam outlet is connected with the second-effect falling-film evaporator through a pipeline and is used for sending secondary steam generated by the first-effect falling-film evaporator into the second-effect falling-film evaporator to be used as a heat exchange medium of the second-effect falling-film evaporator; the evaporator further comprises a steam pipeline, wherein the steam pipeline is respectively connected with the steam inlets of the first-effect falling-film evaporator and the third-level falling-film evaporator and is used as a heat exchange medium of the first-effect falling-film evaporator and the third-level falling-film evaporator.
More specifically: the single-effect falling film evaporator comprises a single-effect falling film heat exchanger 33, a single-effect circulating pipeline, a single-effect circulating pump 40 and a single-effect falling film evaporation chamber 34, wherein the single-effect circulating pipeline is further provided with two control valves and a flowmeter, one of the two control valves and the flowmeter is arranged on one side, close to the single-effect falling film heat exchanger 33, of the single-effect circulating pump 40, and the other control valve is arranged on one side, close to the single-effect falling film evaporation chamber, of the single-effect circulating pump 40. The preheater 32 is communicated with the top end of the tube pass of the single-effect falling film heat exchanger 33 through a pipeline, the bottom end of the tube pass of the single-effect falling film heat exchanger 33 is communicated with the lower end of the single-effect falling film evaporation chamber 34 (specifically communicated through a pipeline, one end of the pipeline is connected with the bottom end of the tube pass of the single-effect falling film heat exchanger 33, the other end of the pipeline is communicated with the single-effect circulating pipeline, and the communication point is located between the single-effect circulating pump 40 and another control valve), the upper end of the tube pass of the single-effect falling film heat exchanger 33 is communicated with the bottom end of the single-effect falling film evaporation chamber 34 through the single-effect circulating pipeline, and the top end of the single-effect falling film evaporation chamber 33 is provided with the single.
The double-effect falling film evaporator comprises a double-effect falling film heat exchanger 35, a double-effect circulating pipeline, a double-effect circulating pump 42 and a double-effect falling film evaporation chamber 36, wherein the double-effect circulating pump 42 and the double-effect falling film evaporation chamber 36 are arranged on the double-effect circulating pipeline, two control valves and a flowmeter are further arranged on the double-effect circulating pipeline, one control valve and the flowmeter are arranged on one side, close to the double-effect falling film heat exchanger 35, of the double-effect circulating pump 42, and the other control valve is arranged on one side, close to the double-effect falling film evaporation chamber 36, of. The lower end of the double-effect falling film evaporation chamber 36 is communicated with the bottom end of the tube pass of the double-effect falling film heat exchanger 35 (specifically, the lower end of the tube pass is communicated with the bottom end of the tube pass of the double-effect falling film heat exchanger 35 through a pipeline, the other end of the pipeline is communicated with a double-effect circulating pipeline, and the communication point is located between a double-effect circulating pump 42 and another control valve), the upper end of the tube pass of the double-effect falling film heat exchanger 35 is communicated with the bottom end of the double-effect falling film evaporation chamber 36 through the double-effect circulating pipeline, the lower end of the first-effect falling film evaporation chamber 34 is communicated with the upper end of the tube pass of the double-effect falling film heat exchanger 35, and the top end of the double-effect falling film evaporation chamber 36 is;
the three-stage falling film evaporator comprises a triple-effect falling film heat exchanger 37, a triple-effect circulating pipeline, a triple-effect circulating pump 43 arranged on the triple-effect circulating pipeline and a triple-effect falling film evaporation chamber 38, wherein the triple-effect circulating pipeline is also provided with two control valves and a flowmeter, one of the two control valves and the flowmeter is arranged on one side of the triple-effect circulating pump 43 close to the triple-effect falling film heat exchanger 37, and the other control valve is arranged on one side of the triple-effect circulating pump 43 close to the triple-effect falling film evaporation chamber 37. The lower end of the triple-effect falling film evaporation chamber 38 is communicated with the bottom end of the tube pass of the triple-effect falling film heat exchanger 37 (specifically, the lower end of the tube pass is communicated with the bottom end of the tube pass of the triple-effect falling film heat exchanger 37 through a pipeline, the other end of the pipeline is communicated with a triple-effect circulating pipeline, and the communicating point is located between a triple-effect circulating pump 43 and another control valve), the upper end of the tube pass of the triple-effect falling film heat exchanger 37 is communicated with the bottom end of the triple-effect falling film evaporation chamber 38 through a triple-effect circulating pipeline, the lower end of the double-effect falling film evaporation chamber 36 is communicated with the upper end of the tube pass of the triple-effect falling film heat exchanger 37 (specifically, the lower end of the double-effect falling film evaporation chamber 36 is communicated with the triple-effect circulating pipeline through a pipeline), and a triple-effect secondary steam outlet.
Still further, falling film evaporation system Q3The double-effect falling film evaporator further comprises a first condensate water tank 41 and a second condensate water tank 44, wherein the first condensate water tank 41 is used for receiving secondary steam generated by the double-effect falling film evaporation chamber 36 and the triple-effect falling film evaporation chamber 38 and condensate water generated in the shell of the double-effect falling film heat exchanger 35, and the second condensate water tank 44 is used for receiving condensate water generated in the shell of the single-effect falling film heat exchanger 33 and the shell of the triple-effect falling film heat exchanger 37. The second condensate tank 44 is connected to the preheater 32, and is configured to introduce the condensate into the preheater 32 as a heat exchange medium for the aluminum sulfate solution, so as to heat the aluminum sulfate solution.
The specific materials and specifications of the two-effect three-stage falling-film evaporator and the preheater in the embodiment are as follows: an effective falling film heat exchanger 33 and an effective falling film evaporation chamber 34
Double-effect falling film heat exchanger 35 and double-effect falling film evaporation chamber 36
Triple effect falling film heat exchanger 37 and triple effect falling film evaporation chamber 38
First-stage preheater
Two-stage preheater
The method for treating the nitric acid wastewater containing the aluminum nitrate based on the nitric acid wastewater containing the aluminum nitrate treatment system has the following design parameters:
the feed concentration of the nitric acid wastewater containing aluminum nitrate is as follows: the acidity is 1.275mol/L.
Feeding temperature of nitric acid wastewater containing aluminum nitrate: 20 deg.C
Feeding amount of nitric acid wastewater containing aluminum nitrate: 10T/h
Evaporation amount of aluminum sulfate solution: 5.688T/h
Evaporation temperature of aluminum sulfate solution: 55-90 deg.C (gas phase temperature, two-stage/three-stage 55 deg.C, and one-stage 90 deg.C)
Boiling point of saturated solution is increased: less than or equal to 46 DEG C
Discharging material state: aluminum sulfate octadecahydrate
Make-up steam pressure: 0.1MPa
Supplementary steam flow: 3913Kg/Hr (determined by design)
Circulating cooling water inlet water temperature: less than or equal to 32 DEG C
Return water temperature of circulating cooling water: less than or equal to 37 DEG C
Circulating cooling water inlet pressure: 0.2-0.5MPa
The return water pressure of the circulating cooling water is as follows: 0-0.1MPa
Flow rate of circulating cooling water: 380T/h (determined by design)
Compressed air pressure: at normal temperature not lower than 0.8MPa, no dust and no oil
Power source capacity: 380V50Hz 4 line 125KVA
The occupied area is as follows: square meter not greater than 450 (can be determined by design)
Height of the equipment: less than or equal to 25 m (as determined by design)
Ambient temperature: 5-35 deg.C
Ambient humidity: 30 to 85 percent
Average air pressure: 101Kpa
Seismic intensity: not more than 7 DEG C
Ambient wind speed: less than or equal to 5 m/s.
The method comprises the following steps:
pumping nitric acid wastewater containing aluminum nitrate in an aluminum nitrate tank to a two-stage column separation system through an aluminum nitrate pump 6, specifically pumping the nitric acid wastewater into a column A, wherein the column A is used as a first-stage column, a column B is used as a second-stage column, a column C is used as a third-stage column, the nitric acid wastewater containing aluminum nitrate enters through a feed inlet of the first-stage column, flows out from a lower series connection port of the first-stage column and enters a feed inlet of the second-stage column, and then flows out from a lower port of the second-stage column and enters a recycling nitric acid tank; when the aluminum content in the effluent liquid of the lower series connection interface of the primary column is more than 80 percent of the aluminum content in the nitric acid wastewater containing aluminum nitrate) the aluminum content in the nitric acid wastewater containing aluminum nitrate indicates that the primary column is saturated (about 2 times of volume, namely the volume of resin contained in each resin column is half of the feeding volume of the column), a series connection pipeline A for connecting the lower series connection interface of the primary column and the upper series connection interface of the secondary column is closed, liquid in the primary column is put back to the aluminum nitrate tank 5, after being dried, the cleaning and the drying are repeated, sulfuric acid with the mass concentration of 30 percent is fed to analyze aluminum ions, after the analysis is finished, the primary column is put into an aluminum sulfate solution tank 13, when the concentration of the aluminum ions detected at an aluminum sulfate solution outlet is close to 0, the sulfuric acid in the resin columns is basically sulfuric acid, and the sulfuric acid is discharged into a sulfuric acid tank through a sulfuric acid outlet and then dried, and;
step two, pumping the aluminum sulfate solution introduced into the aluminum sulfate solution tank 13 in the step one to an aluminum sulfate feeding tank 18 through an aluminum sulfate raw material pump 14, wherein the temperature of the aluminum sulfate solution is not less than 20 ℃ (the temperature under natural conditions), pressurizing the aluminum sulfate solution through a feeding pump 19, then preheating the aluminum sulfate solution to 64 +/-3 ℃, then entering a two-effect three-stage falling-film evaporator for evaporation and concentration to obtain a concentrated solution, entering a cooling crystallization tank through a three-effect circulating pump 43, entering a middle-stage crystallization tank 21 after primary cooling and crystallization, entering a filter press for filter pressing and separation after aluminum sulfate is fully separated out and crystallized, putting solid into a high-level tank, wherein the high-level tank comprises a high-level tank A/B22 (the high-level tank A/B refers to the high-level tank A and the high-level, a higher tank C/D23 (higher tank C/D means higher tank C and higher tank D) and a higher tank E21. Adding aluminum hydroxide into each high-level tank, heating to neutralize residual sulfuric acid, scraping to discharge materials or discharging aluminum sulfate solution after neutralization is finished, and feeding mother liquor separated by filter pressing into a second sulfuric acid tank 15 for later use. The elevated tank is provided with an interlayer, and steam can be introduced into the interlayer for heat exchange, so that the temperature rise of the aluminum sulfate inside is realized. Wherein the head tank E21 may also be used as a transfer tank for receiving neutralized material from the remaining head tanks.
And step three, closing the series pipeline A and simultaneously opening the series pipeline B, using the column B as a new first-stage column, using the column C as a new second-stage column and using the column D as a new third-stage column, and repeating the operation in the step one and the step two. And (3) closing the series pipeline B after the column B is saturated, simultaneously opening the series pipeline C, using the column C as a new first-stage column, using the column D as a new second-stage column and using the column A as a new third-stage column, and repeating the operation in the first step and the second step. And (3) closing the series C pipeline after the column C is saturated, simultaneously opening the series D pipeline, using the column D as a new first-stage column, using the column A as a new second-stage column and using the column B as a new third-stage column, and repeating the operation in the first step and the second step.
And step four, closing the D series pipeline after the D column is saturated, simultaneously opening the A series pipeline, and repeating the operations in the step one, the step two to the step three until the column separation and analysis of all the nitric acid wastewater containing aluminum nitrate are completed.
Further, the specific method for repeatedly cleaning and drying the primary column before sulfuric acid analysis in the primary column in the step one comprises the following steps: firstly, pumping dilute nitric acid in a dilute nitric acid tank 9 into a cleaning water inlet by a dilute nitric acid pump 10 to enter a primary column for dilute nitric acid displacement, completely discharging the dilute nitric acid into the dilute nitric acid tank 9 after displacement, and then blowing to dry; and pumping the water in the cleaning water tank 3 into a cleaning water inlet by a cleaning water pump 4, then entering a primary column for water replacement, discharging all the water into a dilute nitric acid tank 9 after the water replacement, and drying the water.
The specific method for repeatedly cleaning and drying the primary column after sulfuric acid analysis is carried out on the primary column in the step one comprises the following steps: firstly pumping dilute sulfuric acid in a dilute sulfuric acid tank 11 into a cleaning water inlet by a dilute sulfuric acid pump 12 so as to enter a primary column, performing dilute sulfuric acid replacement, completely discharging the dilute sulfuric acid into the dilute sulfuric acid tank 11 after the replacement, and then blowing dry the primary column; and then pumping the water in the cleaning water tank 3 into a cleaning water inlet by a cleaning water pump 4 so as to enter a primary column for water replacement, completely discharging the water into a dilute sulfuric acid tank 11 after the water replacement, and drying the primary column for later use.
Further, the specific method for evaporating and concentrating the aluminum sulfate solution by the two-effect three-stage falling-film evaporator in the third step comprises the following steps: the aluminum sulfate solution firstly enters the tube pass of the first-effect falling film heat exchanger 33, the material in the tube pass of the first-effect falling film heat exchanger exchanges heat with the heating steam in the shell layer of the first-effect falling film heat exchanger for boiling evaporation, part of liquid drops carried by the water vapor generated by evaporation enter the first-effect falling film evaporation chamber 34, the water vapor forms the secondary steam after the liquid drops in the water vapor are separated out by the first-effect falling film evaporation chamber 34, the secondary steam enters the shell layer of the second-effect falling film heat exchanger 35, one part of the liquid drops separated out by the first-effect falling film evaporation chamber 34 is pumped by the first-effect circulating pipeline to flow back to the tube pass of the first-effect falling film heat exchanger 33 for continuous heating and concentration, the other part of the first-effect concentrated solution is pumped by the first-effect circulating pump to the tube pass of the second-effect falling film heat exchanger 35 and exchanges heat with the secondary steam in the shell layer of the second-effect falling film heat exchanger 35 for further, the water vapor generated by evaporation carries part of liquid drops into the double-effect falling film evaporation chamber 36, and the water vapor forms secondary steam after the liquid drops in the water vapor are separated from the water vapor by the double-effect falling film evaporation chamber 36; one part of the liquid drops separated by the double-effect falling film evaporation chamber is pumped by a double-effect circulating pipeline and flows back to the tube pass of the double-effect falling film heat exchanger 35 for continuous heating and concentration, the other part of the liquid drops is the double-effect concentrated liquid, the double-effect concentrated liquid is pumped by a double-effect circulating pump to the tube pass of the triple-effect falling film heat exchanger 37 and exchanges heat with heating steam in the shell layer of the triple-effect falling film heat exchanger 37 for boiling evaporation, part of the liquid drops carried by the water vapor generated by the evaporation enter the triple-effect falling film evaporation chamber 38, the water vapor is separated from the liquid drops in the triple-effect falling film evaporation chamber 38 to form secondary steam, the secondary steam can enter a first condensation water tank 41 together with the secondary steam discharged by the double-effect falling film evaporation chamber 36 and condensed water generated in the shell layer of the double-effect falling film heat exchanger 35, and condensed water generated in the shell layers of the single-effect falling film heat exchanger and the triple-effect falling film heat exchanger, the condensate water in the second condensate tank 44 is finally pressed into the preheater 32 and, after heat exchange with the aluminium sulphate solution, into the V-01 condensate tank 47.
Based on the above system and method for treating nitric acid wastewater containing aluminum nitrate, the cost evaluation of treating 10T nitric acid waste liquid containing aluminum nitrate per hour is as follows:
comparison conditions
Working time: the number of the culture medium is 330 days/year, 24 hours/day,
electricity price: 0.82 yuan/KWh steam number: 195 yuan/ton
Industrial circulating water: boiling point of 0.1 yuan/ton saturated solution is increased: less than or equal to 43 ℃ (saturated solution means that when the content of sulfuric acid in aluminum sulfate is increased to 55% or more, a large amount of aluminum sulfate can be separated out by cooling)
Price of 98% sulfuric acid: 337.8 yuan/ton; price of 8% nitric acid: 188.2 yuan/ton
Evaporation power: steam evaporation capacity: 5.688T/h
10T/h resin column operation cost table
10T/h evaporation concentration operation cost table
10T/h evaporator operation recovery by-product table
The cost and income per hour are calculated, so that 139.36 yuan can be generated per ton, and the graphite evaporator is adopted, so that the corrosion problem of equipment is avoided, the problem of acid wastewater is solved, and the income is created. The design scheme fully considers the influence of factors such as material components, dirt and the like on the power consumption of the system in the actual operation engineering of the system, certain allowance is left for design parameters and equipment configuration, and economic benefits are generated while wastewater is treated.
In light of the foregoing, it will be apparent to those skilled in the art from this disclosure that various changes and modifications can be made without departing from the spirit and scope of the invention. The technical scope of the present invention is not limited to the content of the specification, and must be determined according to the scope of the claims.
Claims (8)
1. The utility model provides a nitric acid effluent disposal system who contains aluminium nitrate which characterized in that: the method comprises the following steps:
the two-stage column-passing separation system is used for separating out aluminum ions in the nitric acid wastewater containing aluminum nitrate and comprises at least 3 resin columns and serial pipelines with the same number as the resin columns, an upper serial connection port, a feed inlet, a compressed air inlet, a cleaning water inlet and a sulfuric acid inlet are arranged at the top ends of the resin columns in parallel, and a lower serial connection port, an aluminum sulfate solution outlet, a nitric acid waste liquid outlet and a nitric acid wastewater outlet containing aluminum nitrate are arranged at the bottom ends of the resin columns in parallel; the resin columns are sequentially connected in series through the series pipelines connected between the lower series connection interface and the upper series connection interface to form a loop;
the aluminum nitrate tank is provided with a liquid outlet connected with the feed inlet and a liquid return port connected with the nitric acid wastewater outlet containing aluminum nitrate;
the device also comprises a compressed air pipeline connected with the compressed air inlet, a cleaning water tank connected with the cleaning water inlet, a sulfuric acid tank connected with the sulfuric acid inlet, and an aluminum sulfate solution tank connected with the aluminum sulfate solution outlet;
the system comprises an aluminum sulfate feeding tank, a preheater, a double-effect three-stage falling-film evaporator for evaporating and concentrating aluminum sulfate solution for multiple times, a cooling crystallization tank, a crystallization transfer tank, a pressure filter, a high-level tank for receiving the solid after pressure filtration and a scraping machine which are connected in sequence; the aluminum sulfate feeding tank is connected with the aluminum sulfate solution tank.
2. The aluminum nitrate-containing nitric acid wastewater treatment system according to claim 1, wherein: the resin column has 4, is A post, B post, C post and D post respectively, the series connection pipeline has 4, is being used for the A series connection pipeline of being connected the lower series connection interface of A post and the last string connection mouth of B post respectively, is used for the B series connection pipeline of being connected the lower series connection interface of B post and the last string connection mouth of C post, is used for the C series connection pipeline of being connected the lower series connection interface of C post and the last string connection mouth of D post to and be used for the D series connection pipeline of being connected the lower series connection interface of D post and the last string connection mouth of A post.
3. The aluminum nitrate-containing nitric acid wastewater treatment system according to claim 1, wherein: the device also comprises a recycling nitric acid tank connected with the nitric acid waste liquid outlet, a dilute nitric acid outlet is connected to the lower end of the resin column in parallel, and the dilute nitric acid outlet is connected with a dilute nitric acid tank and used for receiving dilute nitric acid discharged by water replacement before aluminum ion desorption in the resin column; the dilute nitric acid tank is also connected with the cleaning water inlet of the resin column and is used for introducing dilute nitric acid into the resin column for replacement;
and/or the lower end of the resin column is also provided with a dilute sulfuric acid outlet in parallel, and the dilute sulfuric acid outlet is connected with a dilute sulfuric acid tank and used for receiving dilute sulfuric acid discharged by water replacement after aluminum ions are desorbed in the resin column; and the dilute sulfuric acid tank is connected with the cleaning water inlet of the resin column and is used for introducing dilute sulfuric acid into the resin column for replacement.
4. The aluminum nitrate-containing nitric acid wastewater treatment system according to claim 1, wherein: the bottom of the resin column is connected in parallel with a sulfuric acid outlet, and the sulfuric acid outlet is connected with a sulfuric acid tank.
5. The aluminum nitrate-containing nitric acid wastewater treatment system according to claim 1, wherein: the two-effect three-stage falling-film evaporator comprises:
the first-effect falling film evaporator is used for carrying out first-effect falling film evaporation on the aluminum sulfate solution preheated by the preheater to form first-effect concentrated solution;
the double-effect falling film evaporator is used for carrying out double-effect falling film evaporation on the primary-effect concentrated solution from the primary-effect falling film evaporator to form a double-effect concentrated solution;
the three-level falling film evaporator is used for carrying out triple-effect falling film evaporation on the double-effect concentrated solution from the double-effect falling film evaporator to form triple-effect concentrated solution;
the first-effect falling-film evaporator is provided with a first-effect secondary steam outlet, the first-effect secondary steam outlet is connected with the second-effect falling-film evaporator through a pipeline and is used for sending secondary steam generated by the first-effect falling-film evaporator into the second-effect falling-film evaporator to be used as a heat exchange medium of the second-effect falling-film evaporator; the evaporator further comprises a steam pipeline, wherein the steam pipeline is respectively connected with the steam inlets of the first-effect falling-film evaporator and the third-level falling-film evaporator and is used as a heat exchange medium of the first-effect falling-film evaporator and the third-level falling-film evaporator.
6. The aluminum nitrate-containing nitric acid wastewater treatment system according to claim 5, wherein: the aluminum sulfate purification system further comprises a first condensate water tank and a second condensate water tank, wherein the first condensate water tank is used for receiving secondary steam generated by the double-effect falling film evaporation chamber and the triple-effect falling film evaporation chamber and condensate water generated in a shell layer of the double-effect falling film heat exchanger, and the second condensate water tank is used for receiving condensate water generated in a shell layer of the single-effect falling film heat exchanger and a shell layer of the triple-effect falling film heat exchanger.
7. The aluminum nitrate-containing nitric acid wastewater treatment system according to claim 6, wherein: and the second condensate water tank is connected with the preheater and is used for introducing condensate water into the preheater to be used as a heat exchange medium of the aluminum sulfate solution.
8. The aluminum nitrate-containing nitric acid wastewater treatment system according to claim 1, wherein: the heat exchanger further comprises a first heat exchanger, wherein a tube pass inlet and a tube pass outlet of the first heat exchanger are connected with the high-level tank and used for condensing and refluxing hot steam generated by the high-level tank.
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Address after: 213000, No. 16 Donggang Second Road, Weicun Street, Xinbei District, Changzhou City, Jiangsu Province Patentee after: Changzhou Zhongyuan Technology Co.,Ltd. Country or region after: China Address before: 213126 No.82, Anjia Zhenxing Road, Chunjiang Town, Xinbei District, Changzhou City, Jiangsu Province Patentee before: CHANGZHOU ZHONGYUAN ENGINEERING TECHNOLOGY Co.,Ltd. Country or region before: China |