CN103359865A - Energy-saving environment-friendly nitrification wastewater treatment method - Google Patents
Energy-saving environment-friendly nitrification wastewater treatment method Download PDFInfo
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- CN103359865A CN103359865A CN2013102805621A CN201310280562A CN103359865A CN 103359865 A CN103359865 A CN 103359865A CN 2013102805621 A CN2013102805621 A CN 2013102805621A CN 201310280562 A CN201310280562 A CN 201310280562A CN 103359865 A CN103359865 A CN 103359865A
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- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 11
- 239000002351 wastewater Substances 0.000 claims abstract description 120
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 85
- 238000001816 cooling Methods 0.000 claims abstract description 65
- 238000000034 method Methods 0.000 claims abstract description 42
- 239000003513 alkali Substances 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000002425 crystallisation Methods 0.000 claims abstract description 19
- 230000008025 crystallization Effects 0.000 claims abstract description 19
- 239000002253 acid Substances 0.000 claims abstract description 18
- 238000001914 filtration Methods 0.000 claims abstract description 11
- 238000006386 neutralization reaction Methods 0.000 claims description 53
- 238000005406 washing Methods 0.000 claims description 46
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 claims description 36
- 238000006396 nitration reaction Methods 0.000 claims description 28
- 150000001875 compounds Chemical class 0.000 claims description 20
- 230000008569 process Effects 0.000 claims description 16
- WDCYWAQPCXBPJA-UHFFFAOYSA-N 1,3-dinitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC([N+]([O-])=O)=C1 WDCYWAQPCXBPJA-UHFFFAOYSA-N 0.000 claims description 13
- 230000007935 neutral effect Effects 0.000 claims description 10
- LQNUZADURLCDLV-UHFFFAOYSA-N nitrobenzene Chemical compound [O-][N+](=O)C1=CC=CC=C1 LQNUZADURLCDLV-UHFFFAOYSA-N 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 8
- 229920006395 saturated elastomer Polymers 0.000 claims description 8
- 238000012856 packing Methods 0.000 claims description 3
- 239000011800 void material Substances 0.000 claims description 3
- IQUPABOKLQSFBK-UHFFFAOYSA-N 2-nitrophenol Chemical compound OC1=CC=CC=C1[N+]([O-])=O IQUPABOKLQSFBK-UHFFFAOYSA-N 0.000 abstract description 41
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 238000000605 extraction Methods 0.000 abstract description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract description 5
- 238000006722 reduction reaction Methods 0.000 abstract description 4
- 239000000463 material Substances 0.000 abstract description 3
- 230000009467 reduction Effects 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 239000003344 environmental pollutant Substances 0.000 abstract description 2
- 231100000719 pollutant Toxicity 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 230000003472 neutralizing effect Effects 0.000 abstract 8
- 150000004767 nitrides Chemical class 0.000 abstract 4
- 238000001179 sorption measurement Methods 0.000 abstract 2
- 101100298222 Caenorhabditis elegans pot-1 gene Proteins 0.000 description 17
- 238000004519 manufacturing process Methods 0.000 description 12
- VLZLOWPYUQHHCG-UHFFFAOYSA-N nitromethylbenzene Chemical compound [O-][N+](=O)CC1=CC=CC=C1 VLZLOWPYUQHHCG-UHFFFAOYSA-N 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 239000010865 sewage Substances 0.000 description 9
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 7
- 241001529739 Prunella <angiosperm> Species 0.000 description 6
- VYZAHLCBVHPDDF-UHFFFAOYSA-N Dinitrochlorobenzene Chemical compound [O-][N+](=O)C1=CC=C(Cl)C([N+]([O-])=O)=C1 VYZAHLCBVHPDDF-UHFFFAOYSA-N 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 5
- SLVBYWGNYOLBEU-UHFFFAOYSA-N C1(=CC=CC=C1)O.[N+](=O)([O-])C1=C(C=CC=C1)[N+](=O)[O-] Chemical compound C1(=CC=CC=C1)O.[N+](=O)([O-])C1=C(C=CC=C1)[N+](=O)[O-] SLVBYWGNYOLBEU-UHFFFAOYSA-N 0.000 description 4
- XZQLMDHYBJHUJU-UHFFFAOYSA-N [N+](=O)([O-])CC1=CC=CC=C1.C1(=CC=CC=C1)O Chemical compound [N+](=O)([O-])CC1=CC=CC=C1.C1(=CC=CC=C1)O XZQLMDHYBJHUJU-UHFFFAOYSA-N 0.000 description 4
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000002594 sorbent Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 150000002828 nitro derivatives Chemical class 0.000 description 3
- XLQKZHYPTYWOFK-UHFFFAOYSA-N C1(=CC=CC=C1)O.[N+](=O)([O-])C=1C(=C(C=CC1)Cl)[N+](=O)[O-] Chemical compound C1(=CC=CC=C1)O.[N+](=O)([O-])C=1C(=C(C=CC1)Cl)[N+](=O)[O-] XLQKZHYPTYWOFK-UHFFFAOYSA-N 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- CDAWCLOXVUBKRW-UHFFFAOYSA-N 2-aminophenol Chemical compound NC1=CC=CC=C1O CDAWCLOXVUBKRW-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000002147 killing effect Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- Physical Water Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses an energy-saving environment-friendly nitrification wastewater treatment method. The nitride and nitrification neutralizing wastewater from a neutralizing reaction pot enter an oil-water separator; the nitride at the lower layer of the oil-water separator goes to a follow-up nitride section, and the nitrification neutralizing wastewater at the upper layer of the oil-water separator enters a cooling tower for cooling and then enters a filter; nitrophenolate separated by crystallization from the nitrification neutralizing wastewater is recovered in the filter; the filtered stock after filtering enters a heater and is heated to the neutralizing temperature required by the neutralizing reaction pot; and the heated filtered stock containing enough alkali and with low phenol content is neutralized with the acid nitride in the neutralizing pot. According to the method disclosed by the invention, the recovery of nitrophenolate in the nitrification wastewater and the treatment of nitrification neutralizing wastewater are realized by use of the solubility-temperature relation of the nitrophenolate; the energy is saved by over 90% than the methods of adsorption, concentration, extraction and the like; and compared with the methods of iron powder reduction, adsorption, extraction and the like, the consumption of auxiliary chemical materials is avoided, the nitrophenolate is recovered to turn waste into wealth, and the transfer of secondary pollutants is avoided.
Description
Technical field
The present invention relates to method of wastewater treatment, particularly method of wastewater treatment in a kind of nitrated production process.
Background technology
Nitration reaction is to use very wide reaction member in the chemical process.In the nitration reaction production process of benzene, chlorobenzene or toluene, after nitration reaction is finished, nitro-compound need to be separated mutually with acid, for the ease of subsequent disposal, need to neutralize to acid nitro-compound, nitro produce thing reaches neutral or omits meta-alkalescence in the middle of making.In N-process, partial nitro thing generation hydrolysis reaction generates nitrophenol, and nitrophenol and alkali reaction generate the nitro phenates simultaneously, and the nitro phenates is soluble in water, forms to contain in nitro phenates nitrated and waste water.
Phenolic wastewater is a kind of wide material sources, the serious trade effluent of harm.And nitrophenol contains the strong electron-withdrawing group nitro owing in the molecular structure, so that cloud density descends greatly on the phenyl ring, stability strengthens, and at the occurring in nature hard degradation, the processing that contains nitrophenol wastewater still is the difficult problem in the sewage disposal at present.Therefore researching and developing the treatment process and the device that contain nitrophenol wastewater has great importance.
Many chemical industrial parks all have the sewage centralized processor, this class sewage centralized processor has certain requirement except the COD value to the sewage that enters system, composition to waste water has strict requirement especially, the sewage that contains bio-toxicity has killing action to the biological bacterium of centralized processor, therefore, the sewage centralized processor all requires sewage generation unit that raw waste water is carried out pre-treatment, otherwise can not enter unified Sewage treatment systems.The waste water that contains nitro-compound is then strictly kept outside of the door.
At present, the method that many improvement nitration waste waters have been arranged, typical method has: (1) method of enrichment, adopt the method for evaporation, nitrophenol is condensed into solid, and solid product goes to solid powder treatment plant to process or solid is burned, because nitrophenol content is generally all very low in the waste water, need to consume a large amount of heats when concentrated, the cost of wastewater treatment is very high.In addition, nitrophenol at high temperature is very unsettled compound, and the danger of blast is arranged in the evaporating concentration process.(2) reduction method, this method becomes amino with the nitroreduction in the nitrophenol, usually adopts iron powder reducing technique, and the waste water that will contain nitrophenol is converted into the waste water that contains amino phenol, further carries out biochemical degradation again.The front points out, nitrophenol content is very low in the waste water, and thorough in order to make reduction reaction, iron powder is excessive in a large number, generates the iron mud that is difficult to process in the reduction process, causes secondary pollution.(3) absorption method is selected certain sorbent material, and nitrophenol is adsorbed on the sorbent material, again by desorption method solution sucking-off nitrophenol.(4) extraction process, this method extracts the nitrophenol in the waste water by selecting suitable extraction agent.(3), the high and sorbent material of (4) two kinds of techniques ubiquity energy consumption in desorb and extraction agent removal process, problem that loss of extractant is high.Also there is the secondary pollution problem of the sorbent material of scrapping in absorption method.(5) supercritical catalyst oxidizing process, this method is carried out under greater than the 20MPa condition greater than 400 ℃, pressure in temperature usually, namely utilize organism some physics and chemistry characteristics in supercritical water, with specific oxygenant with the nitrophenol oxidation and be degraded to micromolecular inorganics.Supercritical methanol technology since technique under very high temperature and pressure, manufacturing and the operating requirement of equipment are higher.At high temperature and containing under the condition of strong oxidizer, face the selection difficulty of equipment and instrument in the course of industrialization.In addition, nitration waste water is heated to 400 ℃ of needs from normal temperature and consumes mass energy.(6) electrochemical catalysis cracking, this method efficient is lower, also is difficult to industrialization.
Summary of the invention
For the technical problem that exists in the existing nitration waste water treatment process, the nitration waste water treatment process that the purpose of this invention is to provide a kind of energy-conserving and environment-protective, with nitrophenol in the nitration waste water or nitro phenates with recovered in solid form, Simultaneous Nitrification waste water is re-used in nitrated N-process, realizes the energy-conserving and environment-protective of nitration waste water are processed.
Ultimate principle of the present invention is: the nitro phenates has certain solubleness in water, solubleness increases along with the rising of temperature, and solubleness reduces along with the decline of temperature; When temperature was lower than the temperature of saturation of nitro phenates, the nitro phenates was with regard to crystallization.
Atmospheric temperature or industrial cycle water temp are usually below 35 ℃, the temperature of itrated compound N-process is compared higher with atmospheric temperature or industrial cycle water temp, there is certain temperature head in both, utilize this temperature head, the temperature of envrionment temperature or industrial circulating water will be cooled to be near or below with waste water in nitrated, the nitro phenates will crystallization in nitrated and in the waste water, the nitro phenates of crystallization is filtered, realize the recovery of nitro phenates, simultaneously filtrated stock is added the alkali that neutralization needs and be warmed up to neutralization the temperature that needs and be recycled and reused for N-process.
Blast the air of the water that do not reach capacity in the nitration waste water, unsaturated air with the nitration waste water contact process in reach capacity, take away the part water in the nitration waste water, water in the nitration waste water enters becomes vaporous water in the air event, nitrophenol or nitro phenates are because boiling point is very high, in the air-blowing process, nitrophenol or nitro phenates are still stayed in the nitration waste water; Thereby the vaporization absorption part heat of water reduces the temperature of nitration waste water, and along with the reduction of temperature, the temperature of nitration waste water is lower than the temperature of saturation of nitro phenates, and nitrophenol salts out.
The present invention is for achieving the above object, realize by following technical scheme: from the itrated compound of neutralization reaction pot and nitrated in and waste water enter water-and-oil separator, the phenol itrated compound that contains of water-and-oil separator lower floor removes washing pot, add the nitro phenates in the washing water flush away itrated compound in the washing pot, the itrated compound after the washing goes to follow-up itrated compound workshop section; In water-and-oil separator upper strata nitrated and waste water be that phenolic wastewater enters cooling tower with the phenolic wastewater from washing pot, phenolic wastewater enters from the top of cooling tower, remove strainer from the bottom of cooling tower, unsaturated air enters cooling tower and enters atmosphere from the top of cooling tower after saturated in tower from the bottom of cooling tower; Phenolic wastewater is cooled to certain temperature in cooling tower, cooled phenolic wastewater enters strainer, the nitro phenates of crystallization is recovered in strainer in the phenolic wastewater, the low filtrated stock of the phenol amount that contains after the filtration enters the neutral temperature that well heater is heated to neutralization reaction pot needs, and filtrated stock is added the alkali number that neutralization needs in heat-processed; The low filtrated stock of the phenol amount that contains that contains enough alkali contents after the heating and acid itrated compound be neutralization in neutralization pot, the recovery that realizes the nitro phenates with nitrated in the reusing of waste water.
Wherein, cooling tower is tray column or packing tower or void tower.
Wherein, the neutral temperature of oil of mirbane is at 50-70 ℃, and the neutral temperature of dinitrobenzene is at 80-95 ℃.
The present invention has the following advantages: (1) energy consumption is low, without the heat of phase transformation of large water gaging, compares energy-conservation more than 90% than methods such as absorption, concentrated, extractions in the process; (2) compare with methods such as iron powder reducing, absorption, extractions, without the assistant chemical materials consumption; (3) rate of recovery of nitro phenates is high, turns waste into wealth, and avoids secondary pollutant to shift; (4) sewage load is few; (5) required equipment is simple, reduced investment, processing ease.
Description of drawings
Fig. 1 is schematic flow sheet of the present invention.
Among the figure: 1 neutralization reaction pot, 2 water-and-oil separators, 3 cooling towers, 4 strainers, 5 well heaters, 6 washing pots.
Embodiment
Below in conjunction with specific embodiment, technical solution of the present invention is described in further detail.Should be understood that these embodiment just in order to demonstrate the invention, but not limit the scope of the invention by any way.Succinct in order to narrate; this specification sheets has omitted the settings such as the valve of routine, instrument on the pipeline; the those of ordinary skill of the industry can design, adjust or improve according to standard, also can adjust number of devices and arrangement form, and these adjustment, improvement all should be considered as protection scope of the present invention.
As shown in Figure 1, from the itrated compound of neutralization reaction pot 1 and nitrated in and waste water enter water-and-oil separator 2, the phenol itrated compound that contains of water-and-oil separator 2 lower floors removes washing pot 6, adds washing water in the washing pot 6, the itrated compound after the washing goes to follow-up itrated compound workshop section; In water-and-oil separator 2 upper stratas nitrated and waste water to be phenolic wastewater enter the top of phenolic wastewater cooling tower 3 and remove strainer 4 from the bottom of cooling tower 3 with phenolic wastewater from washing pot 6, bottom from cooling tower 3 blasts unsaturated air simultaneously, unsaturated air in cooling tower with the phenolic wastewater counter current contact, the top from cooling tower 3 after the air saturation enters atmosphere and takes away part water the phenolic wastewater; Phenolic wastewater is cooled to certain temperature in cooling tower 3, cooled phenolic wastewater enters strainer 4, the nitro phenates of crystallization is recovered in strainer 4 in the phenolic wastewater, filtrated stock after the filtration enters filtrated stock well heater 5 and is heated to the neutral temperature that neutralization reaction pot 1 needs, and filtrated stock is added the alkali number that neutralization needs in heat-processed; The low filtrated stock of the phenol amount that contains that contains enough alkali and acid itrated compound after the heating neutralize in neutralization reaction pot 1, the recovery that realizes the nitro phenates with nitrated in the reusing of waste water.
Wherein, cooling tower 3 is packing tower or tray column or void tower.
Wherein, the neutral temperature of oil of mirbane is at 50-70 ℃, and the neutral temperature of dinitrobenzene is at 80-95 ℃.
Embodiment 1: in nitrated in the oil of mirbane production process and the processing of waste water, carry out according to following steps:
(1) acid oil of mirbane and the low filtrated stock of the phenol amount that contains that contains enough alkali in the neutralization reaction pot 70 ℃ of neutralizations, partial nitro benzene generates nitrophenol, nitrophenol and alkali reaction become the nitro phenates simultaneously, oil of mirbane after the neutralization enters water-and-oil separator 2 with phenolic wastewater, the phenol oil of mirbane that contains of water-and-oil separator 2 lower floors enters washing pot 6, add washing water in the washing pot 6, the itrated compound after the washing enters follow-up workshop section;
(2) water-and-oil separator 2 upper strata phenolic wastewater with mix from the phenolic wastewater in the washing pot 6 after enter the top of cooling tower 3 and remove strainer 4 from the bottom of cooling tower 3, bottom to cooling tower blasts unsaturated air simultaneously, unsaturated air in cooling tower 3 with the phenolic wastewater counter current contact, air enters atmosphere from cat head after saturated cooling tower 3 is interior, phenolic wastewater is cooled to 35 ℃, part nitrophenol sal prunella crystallization in the phenolic wastewater after the cooling;
(3) cooled phenolic wastewater enters filtration unit 4, and through the nitro phenates of filtered and recycled crystallization, the filtrated stock after the filtration enters well heater 5;
(4) in well heater 5, filtrated stock is heated to the required temperature of neutralization reaction pot 1, and filtrated stock adds the required alkali of neutralization in heat-processed;
(5) the low filtrated stock of the phenol amount that contains and the acid oil of mirbane that contain enough alkali neutralize in neutralization reaction pot 1, realize nitrated in and the recirculation utilization of waste water and finish nitrated in and the processing of waste water.
Embodiment 2: the processing of nitration waste water in the nitrated production dinitrobenzene of the benzene production process, carry out according to following steps:
(1) acid dinitrobenzene and the low filtrated stock of the phenol amount that contains that contains enough alkali in the neutralization reaction pot 95 ℃ of neutralizations, the part dinitrobenzene generates nitrophenol, nitrophenol and alkali reaction become the nitro phenates simultaneously, after the neutralization contain the phenol dinitrobenzene with contain phenol nitrated in and waste water enter water-and-oil separator 2, the phenol dinitrobenzene that contains of water-and-oil separator 2 lower floors enters washing pot 6, add washing water in washing pot 6, the dinitrobenzene after the washing enters follow-up workshop section;
(2) water-and-oil separator 2 upper strata phenolic wastewater with enter the top of cooling tower 3 and remove strainer 4 from the bottom of cooling tower 3 after phenolic wastewater in the washing pot 6 mixes, bottom from cooling tower 3 blasts unsaturated air simultaneously, unsaturated air becomes saturated moist air and enters atmosphere from the top of cooling tower 3 with the phenolic wastewater counter current contact in cooling tower 3, phenolic wastewater is cooled to 25 ℃, part nitrophenol sal prunella crystallization in the phenolic wastewater after the cooling;
(3) cooled phenolic wastewater enters strainer 4, and through the nitro phenates of filtered and recycled crystallization, the filtrated stock after the filtration enters well heater 5;
(4) in well heater 5, filtrated stock is heated to the required temperature of neutralization reaction pot 1, and filtrated stock adds the required alkali of neutralization in heat-processed;
(5) the low filtrated stock of the phenol amount that contains that contains enough alkali contents and the acid dinitrobenzene after the heating neutralize in neutralization reaction pot 1, realize nitrated in the recirculation utilization of waste water and finish nitrated in the processing of waste water.
Embodiment 3: the processing of nitration waste water in the nitrated production dinitrobenzene of the benzene production process, carry out according to following steps:
(1) acid dinitrobenzene and the low filtrated stock of the phenol amount that contains that contains enough alkali in the neutralization reaction pot 85 ℃ of neutralizations, the part dinitrobenzene generates nitrophenol, nitrophenol and alkali reaction become the nitro phenates simultaneously, after the neutralization contain the phenol dinitrobenzene with contain phenol nitrated in and waste water enter water-and-oil separator 2, the phenol dinitrobenzene that contains of water-and-oil separator 2 lower floors enters washing pot 6, add washing water in washing pot 6, the dinitrobenzene after the washing enters follow-up workshop section;
(2) water-and-oil separator 2 upper strata phenolic wastewater with enter the top of cooling tower 3 and remove strainer 4 from the bottom of cooling tower 3 after phenolic wastewater in the washing pot 6 mixes, bottom from cooling tower 3 blasts unsaturated air simultaneously, unsaturated air becomes saturated moist air and enters atmosphere from the top of cooling tower 3 with the phenolic wastewater counter current contact in cooling tower 3, phenolic wastewater is cooled to 25 ℃, part nitrophenol sal prunella crystallization in the phenolic wastewater after the cooling;
(3) cooled phenolic wastewater enters strainer 4, and through the nitro phenates of filtered and recycled crystallization, the filtrated stock after the filtration enters well heater 5;
(4) in well heater 5, filtrated stock is heated to the required temperature of neutralization reaction pot 1, and filtrated stock adds the required alkali of neutralization in heat-processed;
(5) the low filtrated stock of the phenol amount that contains that contains enough alkali contents and the acid dinitrobenzene after the heating neutralize in neutralization reaction pot 1, realize nitrated in the recirculation utilization of waste water and finish nitrated in the processing of waste water.
Embodiment 4: the processing of nitration waste water in the Chlorobenzene Nitration production dinitrochlorobenzene production process, carry out according to following steps:
(1) acid dinitrochlorobenzene and the low filtrated stock of the phenol amount that contains that contains enough alkali in the neutralization reaction pot 80 ℃ of neutralizations, the part dinitrochlorobenzene generates nitrophenol, nitrophenol and alkali reaction become the nitro phenates simultaneously, after the neutralization contain the phenol dinitrochlorobenzene with contain phenol nitrated in and waste water enter water-and-oil separator 2, the phenol dinitrochlorobenzene that contains of water-and-oil separator 2 lower floors enters washing pot 6, add washing water in washing pot, dinitrochlorobenzene enters follow-up workshop section after the washing;
(2) water-and-oil separator 2 upper strata phenolic wastewater with enter the top of cooling tower 3 and remove strainer 4 from the bottom of cooling tower after phenolic wastewater in the washing pot 6 mixes, bottom from cooling tower 3 blasts unsaturated air simultaneously, unsaturated air becomes saturated moist air and enters atmosphere from the top of cooling tower 3 with the phenolic wastewater counter current contact in cooling tower 3, phenolic wastewater is cooled to 30 ℃ in cooling tower 3, part nitrophenol sal prunella crystallization in the phenolic wastewater after the cooling;
(3) cooled phenolic wastewater enters strainer 4, and through the nitro phenates of filtered and recycled crystallization, the filtrated stock after the filtration enters well heater 5;
(4) in well heater 5, contain filtrated stock and be heated to the required temperature of neutralization reaction pot 1, filtrated stock adds the required alkali of neutralization in heat-processed;
(5) the low filtrated stock of the phenol amount that contains and the acid dinitrochlorobenzene that contain enough alkali after the heating neutralizes in neutralization reaction pot 1, realize nitrated in the recirculation utilization of waste water and finish nitrated in the processing of waste water.
Embodiment 5: methylbenzene nitration is produced the processing of nitration waste water in the nitrotoluene production process, carries out according to following steps:
(1) acid nitrotoluene and the low filtrated stock of the phenol amount that contains that contains enough alkali in neutralization reaction pot 1 50 ℃ of neutralizations, partial nitro toluene generates nitrophenol, nitrophenol and alkali reaction become the nitro phenates simultaneously, after the neutralization contain the phenol nitrotoluene with contain phenol nitrated in and waste water enter water-and-oil separator 2, the phenol nitrotoluene that contains of water-and-oil separator 2 lower floors enters washing pot 6, add washing water in washing pot 6, the nitrotoluene after the washing enters follow-up workshop section;
(2) water-and-oil separator 2 upper strata phenolic wastewater with enter the top of cooling tower 3 and remove strainer 4 from the bottom of cooling tower 3 after phenolic wastewater in the washing pot 6 mixes, blast unsaturated air from the bottom of cooling tower 3, unsaturated air becomes saturated moist air and enters atmosphere from the top of cooling tower in cooling tower 3 with after the phenolic wastewater counter current contact, phenolic wastewater is cooled to 25 ℃ in cooling tower 3, part nitrophenol sal prunella crystallization in the phenolic wastewater after the cooling;
(3) cooled phenolic wastewater enters strainer 4, and through the nitro phenates of filtered and recycled crystallization, the filtrated stock after the filtration enters well heater 5;
(4) in well heater 5, filtrated stock is heated to the required temperature of neutralization reaction pot 1, and filtrated stock adds the required alkali of neutralization in heat-processed;
(5) the low filtrated stock of the phenol amount that contains that contains enough alkali and the acid nitrotoluene after the heating neutralize in neutralization reaction pot 1, realize nitrated in the recirculation utilization of waste water and finish nitrated in the processing of waste water.
Embodiment 6: methylbenzene nitration is produced the processing of nitration waste water in the nitrotoluene production process, carries out according to following steps:
(1) acid nitrotoluene and the low filtrated stock of the phenol amount that contains that contains enough alkali in neutralization reaction pot 1 60 ℃ of neutralizations, partial nitro toluene generates nitrophenol, nitrophenol and alkali reaction become the nitro phenates simultaneously, after the neutralization contain the phenol nitrotoluene with contain phenol nitrated in and waste water enter water-and-oil separator 2, the phenol nitrotoluene that contains of water-and-oil separator 2 lower floors enters washing pot 6, add washing water in washing pot 6, the nitrotoluene after the washing enters follow-up workshop section;
(2) water-and-oil separator 2 upper strata phenolic wastewater with enter the top of cooling tower 3 and remove strainer 4 from the bottom of cooling tower 3 after phenolic wastewater in the washing pot 6 mixes, blast unsaturated air from the bottom of cooling tower 3, unsaturated air becomes saturated moist air and enters atmosphere from the top of cooling tower in cooling tower 3 with after the phenolic wastewater counter current contact, phenolic wastewater is cooled to 25 ℃ in cooling tower 3, part nitrophenol sal prunella crystallization in the phenolic wastewater after the cooling;
(3) cooled phenolic wastewater enters strainer 4, and through the nitro phenates of filtered and recycled crystallization, the filtrated stock after the filtration enters well heater 5;
(4) in well heater 5, filtrated stock is heated to the required temperature of neutralization reaction pot 1, and filtrated stock adds the required alkali of neutralization in heat-processed;
(5) the low filtrated stock of the phenol amount that contains that contains enough alkali and the acid nitrotoluene after the heating neutralize in neutralization reaction pot 1, realize nitrated in the recirculation utilization of waste water and finish nitrated in the processing of waste water.
Claims (3)
1. the nitration waste water treatment process of energy-conserving and environment-protective, the treatment process that it is characterized in that it may further comprise the steps: from the itrated compound of neutralization reaction pot and nitrated in and waste water enter water-and-oil separator, the phenol itrated compound that contains of water-and-oil separator lower floor removes washing pot, add the nitro phenates in the washing water flush away itrated compound in the washing pot, the itrated compound after the washing goes to follow-up itrated compound workshop section; In water-and-oil separator upper strata nitrated and waste water be that phenolic wastewater enters cooling tower with the phenolic wastewater from washing pot, phenolic wastewater enters from the top of cooling tower, remove strainer from the bottom of cooling tower, unsaturated air enters cooling tower and enters atmosphere from the top of cooling tower after saturated in tower from the bottom of cooling tower; Phenolic wastewater is cooled to certain temperature in cooling tower, cooled phenolic wastewater enters strainer, the nitro phenates of crystallization is recovered in strainer in the phenolic wastewater, the low filtrated stock of the phenol amount that contains after the filtration enters the neutral temperature that well heater is heated to neutralization reaction pot needs, and filtrated stock is added the alkali number that neutralization needs in heat-processed; The low filtrated stock of the phenol amount that contains that contains enough alkali contents after the heating and acid itrated compound be neutralization in neutralization pot, the nitro phenates is recycled and allow nitrated in and waste water reused.
2. the nitration waste water treatment process of energy-conserving and environment-protective according to claim 1, it is characterized in that: cooling tower is tray column or packing tower or void tower.
3. the nitration waste water treatment process of energy-conserving and environment-protective according to claim 1, it is characterized in that: the neutral temperature of oil of mirbane is at 50-70 ℃, and the neutral temperature of dinitrobenzene is at 80-95 ℃.
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| CN107814720A (en) * | 2016-09-14 | 2018-03-20 | 中国石油化工股份有限公司 | A kind of method that nitrobenzene tar recycles |
| CN109095553A (en) * | 2018-10-24 | 2018-12-28 | 广东新会美达锦纶股份有限公司 | A kind of oily-water seperating equipment and method of spinning waste-oil agent |
| CN111603869A (en) * | 2020-06-04 | 2020-09-01 | 湖北东方化工有限公司 | Novel polynitrotoluene dust collection process |
| CN113354007A (en) * | 2021-05-31 | 2021-09-07 | 湖北东方化工有限公司 | Process and device for treating alkaline wastewater in polynitrotoluene production |
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| JP2005349243A (en) * | 2004-06-08 | 2005-12-22 | Babcock Hitachi Kk | Method and apparatus for removing nitrate ion and/or nitrite ion in water to be treated |
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| CN109095553A (en) * | 2018-10-24 | 2018-12-28 | 广东新会美达锦纶股份有限公司 | A kind of oily-water seperating equipment and method of spinning waste-oil agent |
| CN111603869A (en) * | 2020-06-04 | 2020-09-01 | 湖北东方化工有限公司 | Novel polynitrotoluene dust collection process |
| CN113354007A (en) * | 2021-05-31 | 2021-09-07 | 湖北东方化工有限公司 | Process and device for treating alkaline wastewater in polynitrotoluene production |
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| CN103359865B (en) | 2014-09-17 |
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Address after: 223002 Huaian City, Jiangsu province Qingpu District West Road No. 40 Patentee after: Jiangsu Kesheng Intelligent Equipment Co.,Ltd. Address before: 223002 Huaian City, Jiangsu province Qingpu District West Road No. 40 Patentee before: JIANGSU KESHENG CHEMICAL MACHINERY Co.,Ltd. |