CN111039339A - Wastewater treatment system - Google Patents
Wastewater treatment system Download PDFInfo
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- CN111039339A CN111039339A CN202010014305.3A CN202010014305A CN111039339A CN 111039339 A CN111039339 A CN 111039339A CN 202010014305 A CN202010014305 A CN 202010014305A CN 111039339 A CN111039339 A CN 111039339A
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- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 47
- 239000002351 wastewater Substances 0.000 claims abstract description 94
- 230000020477 pH reduction Effects 0.000 claims abstract description 83
- 238000006243 chemical reaction Methods 0.000 claims abstract description 74
- 238000010521 absorption reaction Methods 0.000 claims abstract description 32
- 238000006146 oximation reaction Methods 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims description 81
- 239000002253 acid Substances 0.000 claims description 13
- 238000012546 transfer Methods 0.000 claims description 7
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 3
- 238000007865 diluting Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 56
- 238000000034 method Methods 0.000 abstract description 13
- 230000000694 effects Effects 0.000 abstract description 11
- 230000008569 process Effects 0.000 abstract description 9
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 5
- 239000003513 alkali Substances 0.000 description 41
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 25
- 239000000243 solution Substances 0.000 description 20
- VEZUQRBDRNJBJY-UHFFFAOYSA-N cyclohexanone oxime Chemical compound ON=C1CCCCC1 VEZUQRBDRNJBJY-UHFFFAOYSA-N 0.000 description 16
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 8
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 4
- 238000010276 construction Methods 0.000 description 4
- 230000001590 oxidative effect Effects 0.000 description 4
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000007246 mechanism Effects 0.000 description 3
- 150000002978 peroxides Chemical class 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 3
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 2
- AVXURJPOCDRRFD-UHFFFAOYSA-N Hydroxylamine Chemical compound ON AVXURJPOCDRRFD-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000011790 ferrous sulphate Substances 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 150000003254 radicals Chemical class 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000012028 Fenton's reagent Substances 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 229910017912 NH2OH Inorganic materials 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- -1 ammonia alcohol oxime Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 125000000751 azo group Chemical group [*]N=N[*] 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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Abstract
The invention relates to a wastewater treatment system. The wastewater treatment system comprises: a mixer; the discharge hole of the mixer is communicated with the first feed hole of the acidification reaction kettle; the discharge port of the acidification reaction kettle is communicated with the inlet of the buffer tank; and the tail gas absorption tower is communicated with a first gas outlet of the acidification reaction kettle through a first gas outlet pipeline, and the gas inlet of the tail gas absorption tower is communicated with a second gas outlet of the buffer tank through a second gas outlet pipeline so as to absorb the acidification tail gas generated by the acidification reaction. According to the invention, the stripped wastewater after the oximation reaction is sent into an acidification reaction kettle for acidification reaction so as to pretreat the wastewater, reduce the content of organic matters such as ammonia nitrogen and COD, improve the biodegradability of the wastewater and improve the wastewater treatment effect; the method has the advantages of large wastewater treatment capacity and simple process, and can reduce investment and operation cost by adopting acidification reaction to pretreat the oximation stripping wastewater.
Description
Technical Field
The invention relates to the technical field of chemical wastewater treatment, in particular to a wastewater treatment system.
Background
The wastewater produced by the production process for preparing cyclohexanone oxime by an ammoximation method has the characteristics of high COD, high ammonia nitrogen, high peroxide, low biodegradability and the like, and is a problem in water treatment profession. The wastewater produced by the ammoximation method is large in amount, contains pollutant components such as toluene, cyclohexanone oxime, tert-butyl alcohol, azo compounds, peroxide and the like, is high in COD concentration and low in biodegradability, and the cyclohexanone oxime which is difficult to decompose is an important factor influencing the biochemical treatment of the wastewater, and can cause impact on a wastewater biochemical treatment system when directly discharged into the wastewater biochemical treatment system for biochemical treatment, so that the standard discharge of the wastewater is influenced.
In the existing wastewater pretreatment process, insoluble organic matters, peroxides and the like in the ammoximation wastewater are generally decomposed by utilizing a Fenton reaction mechanism so as to improve the biodegradability of the wastewater, and the wastewater is sent into a biochemical treatment system for further wastewater treatment. The Fenton reaction is ferrous iron (Fe) ion in ferrous sulfate2+) As catalyst and hydrogen peroxide (H)2O2) Oxidation reaction is carried out to treat the waste water. Because the ferrous sulfate and the hydrogen peroxide both have strong redox properties, the Fenton reagent can react to generate hydroxyl free radicals with strong oxidizing property, and the free radicals can oxidize and degrade the structure of insoluble organic pollutants in the wastewater, thereby achieving the aim of oxidizing the pollutantsAnd (4) removing. However, the amount of wastewater treated by the Fenton reaction is small, a large amount of hydrogen peroxide is consumed, and the cost is high; in addition, factors affecting the fenton reaction include: pH, amount of H2O2 added, Fe2+The addition amount, the reaction time, the reaction temperature and the like are difficult to accurately control the reaction, and the wastewater treatment effect is influenced.
Disclosure of Invention
In view of the above problems in the prior art, an object of an aspect of the present invention is to provide a wastewater treatment system for treating oximation wastewater to improve the wastewater treatment capacity and the biodegradability of wastewater, thereby achieving a good wastewater treatment effect.
In order to achieve the above object, the present invention provides a wastewater treatment system for pretreating wastewater of an oximation reaction, comprising:
the mixer is used for mixing the oximation stripping waste water with acid liquor;
the acidification reaction kettle is used for carrying out acidification reaction, and a discharge hole of the mixer is communicated with a first feed hole of the acidification reaction kettle;
the buffer tank is used for storing products after the acidification reaction, and a discharge hole of the acidification reaction kettle is communicated with an inlet of the buffer tank;
and the tail gas absorption tower is communicated with a first gas outlet of the acidification reaction kettle through a first gas outlet pipeline, and the gas inlet of the tail gas absorption tower is communicated with a second gas outlet of the buffer tank through a second gas outlet pipeline so as to absorb the acidification tail gas generated by the acidification reaction.
In some embodiments, the wastewater treatment system further comprises a first liquid return line, wherein the first liquid return line is communicated with the discharge port of the acidification reaction kettle and the second feed port of the acidification reaction kettle.
In some embodiments, the discharge port of the acidification reaction kettle is communicated with the inlet of the buffer tank through a first liquid outlet pipe, the second feed port of the acidification reaction kettle is communicated with the first liquid outlet pipe through the first liquid return pipe, and a first delivery pump is arranged on the first liquid outlet pipe upstream of the first liquid return pipe.
In some embodiments, the PH in the acidification reactor is 1.0 to 5.0, the temperature in the acidification reactor is 55 to 80 ℃, and the pressure in the acidification reactor is atmospheric.
In some embodiments, the wastewater treatment system further comprises an alkali liquor tank, and an alkali liquor outlet of the alkali liquor tank is communicated with an outlet of the buffer tank through an alkali liquor pipeline.
In some embodiments, the outlet of the buffer tank is communicated with an inlet of a wastewater biochemical treatment system through a second liquid outlet pipe, a second delivery pump is arranged on the second liquid outlet pipe, and the alkaline liquid pipe is communicated with an inlet of the second delivery pump through the second liquid outlet pipe.
In some embodiments, the wastewater treatment system further comprises a second liquid return line disposed between the second liquid outlet line downstream of the second delivery pump and the water inlet of the lye tank, for diluting the lye in the lye tank.
In some embodiments, the wastewater treatment system further comprises a heat exchanger disposed on the second effluent line downstream of the second transfer pump.
In some embodiments, a third delivery pump is disposed on the alkaline liquid pipeline at a position close to the alkaline liquid outlet of the alkaline liquid tank, an alkaline liquid branch is connected between the alkaline liquid pipeline and the liquid inlet of the tail gas absorption tower, and the third delivery pump is disposed upstream of the alkaline liquid branch.
In some embodiments, the tail gas absorption tower further comprises a liquid outlet disposed at the bottom of the tail gas absorption tower, the liquid outlet is communicated with an inlet of the buffer tank, and the height of the liquid outlet is higher than the inlet of the buffer tank.
Compared with the prior art, the wastewater treatment system provided by the invention has the advantages that the stripped wastewater after the oximation reaction is sent into the acidification reaction kettle for acidification reaction so as to pretreat the wastewater, so that the content of organic matters such as ammonia nitrogen and COD (chemical oxygen demand) is reduced, the biodegradability of the wastewater is improved, and the wastewater treatment effect is improved. In addition, the oximation stripping wastewater is pretreated by adopting an acidification reaction, the process is simple, the equipment investment of a pretreatment system is reduced, and the construction cost is reduced; in addition, reagents such as an oxidant, a catalyst and the like are not required to be added, so that the consumption of raw materials is greatly reduced, and the cost is reduced.
Drawings
In the drawings, which are not necessarily drawn to scale, like reference numerals may describe similar components in different views. Like reference numerals having letter suffixes or different letter suffixes may represent different instances of similar components. The drawings illustrate various embodiments, by way of example and not by way of limitation, and together with the description and claims, serve to explain the inventive embodiments. The same reference numbers will be used throughout the drawings to refer to the same or like parts, where appropriate. Such embodiments are illustrative, and are not intended to be exhaustive or exclusive embodiments of the present apparatus or method.
FIG. 1 is a schematic view showing the construction of a wastewater treatment system according to an embodiment of the present invention;
reference numerals:
10-stripping waste water, 20-acid liquor, 30-alkali liquor, 40-pretreated waste water and 50-tail gas;
1-a mixer;
2-acidification reaction kettle, 21-first feed inlet, 22-discharge outlet, 23-second feed inlet, 24-first gas outlet, 201-first liquid outlet pipeline, 202-first liquid return pipeline and 203-first gas outlet pipeline;
3-a buffer tank, 31-an inlet, 32-an outlet, 33-a second air outlet, 301-a second liquid outlet pipeline, 302-a bypass liquid outlet pipeline, 303-a second gas outlet pipeline and 304-a second liquid return pipeline;
4-tail gas absorption tower, 41-air inlet, 42-liquid inlet, 43-liquid outlet, 44-noncondensable gas discharge port and 401-absorption liquid outlet pipeline.
51-a first delivery pump, 52-a second delivery pump, 53-a third delivery pump;
6-alkali liquor tank, 601-alkali liquor pipeline, 602-alkali liquor branch;
7-heat exchanger.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the drawings of the embodiments of the present invention.
Unless defined otherwise, technical or scientific terms used herein shall have the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs. The use of "first," "second," and similar terms in the present application do not denote any order, quantity, or importance, but rather the terms are used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that the element or item listed before the word covers the element or item listed after the word and its equivalents, but does not exclude other elements or items. The terms "connected" or "coupled" and the like are not restricted to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "left", "right", and the like are used merely to indicate relative positional relationships, and when the absolute position of the object being described is changed, the relative positional relationships may also be changed accordingly.
To maintain the following description of the embodiments of the present invention clear and concise, a detailed description of known functions and known components of the invention have been omitted.
In the cyclohexanone ammoximation process, ammonia alcohol oxime water which is a reaction product of an oximation reaction kettle is rectified to generate a product cyclohexanone oxime, wastewater containing cyclohexanone generated by the reaction enters a wastewater stripping tower for stripping, stripped wastewater 10 enters a wastewater pretreatment system to reduce the content of organic matters such as ammonia nitrogen, COD and the like, and pretreated wastewater 40 which is pretreated by the wastewater enters a wastewater biochemical treatment system for biochemical treatment so that the treated wastewater meets the discharge standard.
FIG. 1 is a schematic structural view of a wastewater treatment system according to an embodiment of the present invention, in which solid arrows indicate a liquid flow direction (including wastewater and alkali solution), and dotted arrows indicate an exhaust gas flow direction. As shown in fig. 1, an embodiment of the present invention provides a wastewater treatment system for pretreating stripped wastewater 10 of an oximation reaction, the wastewater treatment system comprising:
a mixer 1 for mixing the stripped wastewater 10 with an acid solution 20;
the acidification reaction kettle 2 is used for carrying out acidification reaction, the acidification reaction kettle 2 is provided with a first feeding hole 21 and a discharging hole 22, and the outlet of the mixer 1 is communicated with the first feeding hole 21 of the acidification reaction kettle 2;
the buffer tank 3 is used for storing acidified wastewater after the acidification reaction, the discharge port 22 of the acidification reaction kettle 2 is communicated with the inlet 31 of the buffer tank 3, and the outlet 32 of the buffer tank 3 is communicated with the inlet of a wastewater biochemical treatment system so as to carry out biochemical treatment on pretreated wastewater 40 after acidification and decomposition;
and in the tail gas absorption tower, the gas inlet 41 of the tail gas absorption tower 4 is communicated with the first gas outlet 24 of the acidification reaction kettle through a first gas outlet pipeline 203, and the gas inlet 41 of the tail gas absorption tower 4 is communicated with the second gas outlet 33 of the buffer tank 3 through a second gas outlet pipeline 303 so as to absorb the acidification tail gas generated by the acidification reaction.
According to the wastewater treatment system provided by the embodiment of the invention, the stripped wastewater after the oximation reaction is sent into the acidification reaction kettle 2 for acidification reaction so as to pretreat the wastewater, so that the content of organic matters such as ammonia nitrogen and COD (chemical oxygen demand) is reduced, the biodegradability of the wastewater is improved, and the pretreatment effect of the wastewater is improved. In addition, the acidification reaction is adopted to pretreat the stripping wastewater, the wastewater treatment capacity is large, the process is simple, the equipment investment of a pretreatment system is reduced, and the construction cost is reduced; in addition, reagents such as an oxidant, a catalyst and the like are not required to be added, so that the consumption of raw materials is greatly reduced, and the cost of the raw materials is reduced.
In the embodiment of the invention, the mixer 1, the acidification reaction kettle 2 and the buffer tank 3 are sequentially connected through a pipeline along the wastewater flow direction.
In the embodiment, the stripped wastewater 10 and the acid solution 20 are fed into the mixer 1 to be mixed, and the mixed solution is fed into the acidification reaction kettle 2 to be subjected to acidification reaction, so that the acidification reaction is sufficient, and the wastewater treatment capacity and treatment effect are improved.
The acid solution 20 may be dilutedOne of sulfuric acid, dilute nitric acid, dilute hydrochloric acid and other stronger acids, in this embodiment, the acid solution 20 is preferably sulfur trioxide (SO)3) Oleum (105 acid) at a content of 20%. An acid liquid control valve for adjusting the flow rate of the acid liquid is arranged on the feeding pipeline of the acid liquid 20.
In some embodiments, a PH regulator for detecting PH and a temperature sensor for monitoring temperature are provided in the acidification reaction kettle 2. In a preferred embodiment, the pH value of the acidification reactor 2 is 1.0-5.0, the temperature is 55-80 ℃, and the pressure is normal pressure, so as to provide a better reaction environment for the acidification reaction.
The specific process of the acidification reaction is illustrated by taking the example of the acidification of cyclohexanone oxime, the stripping wastewater 10 can make cyclohexanone oxime contained in the wastewater undergo hydrolysis reaction under the action of an acid solution catalyst through the acidification reaction to generate cyclohexanone and hydroxylamine, and the reaction equation is as follows: c6H10NOH+H2O→C6H10O+NH2OH, the cyclohexanone oxime can be decomposed into biochemically decomposed cyclohexanone by acidification and hydrolysis, so that the content of the cyclohexanone oxime in the wastewater can be reduced, and the wastewater treatment effect is improved.
Further, a stirring mechanism is arranged in the acidification reaction kettle 2, and reaction liquid in the acidification reaction kettle 2 can be uniformly mixed by adopting the stirring mechanism, so that the acidification reaction effect is improved, and the reaction speed is increased.
In some embodiments, as shown in fig. 1, the discharge port 22 of the acidification reactor 2 and the inlet 31 of the buffer tank 3 are communicated through a first liquid outlet pipeline 201, and a first delivery pump 51 is disposed on the first liquid outlet pipeline 201. The acidified wastewater generated after the acidification reaction can be transferred to the buffer tank 3 for storage by the first transfer pump 51.
In some embodiments, the wastewater treatment system further includes a first liquid return pipeline 202, the first liquid return pipeline 202 is disposed at one side of the acidification reactor 2, the first liquid return pipeline 202 is communicated with the discharge port 22 of the acidification reactor 2 and the second feed port 23 of the acidification reactor 2, and a part of the acidified wastewater flowing out from the discharge port 22 after the acidification reaction can be circularly fed into the acidification reactor 2 through the first liquid return pipeline 202 for the acidification reaction until the content parameter of organic matters in the wastewater meets the requirement, so as to improve the acidification reaction efficiency and the reaction effect.
In some embodiments, the first liquid outlet line 201 and the first liquid return line 202 both pump the acidified wastewater after the acidification reaction through the first transfer pump 51, and a flow control valve is respectively disposed on the first liquid outlet line 201 and the first liquid return line 202 to control the flow rate. Specifically, the second feed port 23 of the acidification reactor 2 is communicated with the first liquid outlet pipeline 201 through the first liquid return pipeline 202, and the first liquid outlet pipeline 201 located at the upstream of the first liquid return pipeline 202 is provided with the first delivery pump 51. Can send into buffer tank 3 with the acidizing waste water after the reaction through first delivery pump 51, can flow back acidizing waste water to acidizing reation kettle 2 again, control is convenient, reduces arranging of pump simultaneously, reduce cost.
In some embodiments, the top of the acidification reactor 2 is provided with a first gas outlet 24 for discharging the acidification tail gas generated by the reaction.
The outlet 32 of the buffer tank 3 is connected with the inlet of the wastewater biochemical treatment system through a second liquid outlet pipeline 301, a second delivery pump 52 is arranged on the second liquid outlet pipeline 301, and the acidified wastewater in the buffer tank 3 can be delivered to the wastewater biochemical treatment system through the second delivery pump 52. The top of buffer tank 3 is equipped with second gas outlet 33 for discharge the acidized tail gas in buffer tank 3.
Utilize buffer tank 3 to collect the storage to the acidizing waste water that generates behind the acidizing reaction, be favorable to the centralized processing of waste water on the one hand, on the other hand provides the buffer memory for the subsequent biochemical treatment of waste water, improves the waste water treatment effect.
In some embodiments, as shown in fig. 1, the wastewater treatment system further includes an alkali liquor tank 6 for neutralizing the acidified wastewater generated by the acidification reaction, wherein the alkali liquor 30 is stored in the alkali liquor tank 6, a bottom of the alkali liquor tank 6 is provided with an alkali liquor outlet, the alkali liquor outlet is communicated with the second liquid outlet 301 of the buffer tank 3 through an alkali liquor pipeline 601, the second delivery pump 52 is disposed downstream of the alkali liquor pipeline 601, the alkali liquor 30 output through the alkali liquor pipeline 601 can adjust the PH value of the acidified wastewater discharged from the outlet 32 of the buffer tank 3 to a proper range, and the acidified wastewater (pretreated wastewater 40) adjusted to a certain PH concentration is delivered through the second delivery pump 52, so as to facilitate subsequent wastewater treatment.
Furthermore, a third delivery pump 53 for providing power for delivering the alkali liquor 30 is arranged on the alkali liquor pipeline 601, and the third delivery pump 53 is arranged at a position close to the alkali liquor outlet of the alkali liquor tank 6. The alkali liquor 30 and the acidified wastewater are mixed at the joint of the second liquid outlet pipeline 301 and the alkali liquor pipeline 601 through the third conveying pump 53, and the acidified wastewater adjusted to a certain PH value is conveyed to a wastewater biochemical system through the second conveying pump 52 for further wastewater treatment, so that preparation can be provided for a subsequent wastewater biochemical treatment process, and the wastewater treatment efficiency and effect are improved.
Since the biochemical treatment of wastewater is carried out in an alkaline environment, the pH of the pretreated wastewater 40 is preferably 5 to 10 after the pH is adjusted by adding the alkali solution 30.
In some embodiments, the tail gas absorption tower 4 is filled with an alkali solution 30 for absorbing the acidified tail gas, the alkali solution 30 is from the alkali solution tank 6, an alkali solution branch 602 for conveying the alkali solution 30 is connected between the alkali solution pipeline 601 and the liquid inlet 42 of the tail gas absorption tower 4, and the third conveying pump 53 is disposed upstream of the alkali solution branch 602. A part of the lye 30 in the lye tank 6 can be conveyed to the tail gas absorption tower 4 by the third conveying pump 53 to absorb the acidified tail gas. A liquid outlet 43 is further arranged in the tail gas absorption tower 4, and the liquid outlet 43 of the tail gas absorption tower 4 is arranged at the bottom of the tail gas absorption tower 4 and is communicated with the inlet 31 of the buffer tank 3 through an absorption liquid outlet pipeline 401.
In some embodiments, the wastewater treatment system further comprises a second liquid return line 304 disposed between the second liquid outlet line 301 downstream of the second delivery pump 52 and the water inlet of the lye tank 6, for introducing the wastewater into the lye tank 6 to dilute the lye 30 in the lye tank 60, thereby saving water and improving the wastewater utilization rate. The concentration of the alkali liquor entering from the alkali liquor inlet is about 30 percent, and the alkali liquor 30 is diluted to 1 to 10 percent after the wastewater enters from the water inlet.
Further, tail gas absorption tower 4 sets up in the top of buffer tank 3, and the liquid outlet 43 of tail gas absorption tower 4 highly is higher than the import 31 of buffer tank 3's height for absorption liquid in the tail gas absorption tower 4 can flow into buffer tank 3 automatically, so can cyclic utilization acidizing waste water, pollution abatement.
The top of the tail gas absorption tower 4 is provided with a non-condensable gas discharge port 44 for directly discharging non-condensable gas in the tail gas 50 in the tail gas absorption tower 4.
Through the cooperation of the lye tank 6 and the third delivery pump 53, lye 30 with a certain PH value can be provided for the neutralization of the acidified wastewater, and absorption liquid can be provided for the absorption of the acidified waste gas, so that the process is reasonable and the control is convenient.
In the embodiment of the present invention, the alkali solution 30 for neutralizing the acidified wastewater and the acidified waste gas may be any one of organic alkali and inorganic alkali, as long as the PH of the wastewater can be raised to 5 or more, and in order to reduce the load of the subsequent biochemical treatment of the wastewater, the present invention preferably uses the inorganic alkali solution, and in the embodiment, it is preferable to use 30% sodium hydroxide aqueous solution and dilute the solution to 1-10% by the acidified wastewater.
In some embodiments, as shown in fig. 1, the wastewater treatment system further includes a heat exchanger 7 for cooling the acidified wastewater, the heat exchanger 7 is disposed on the second effluent pipeline 301 downstream of the second delivery pump 52, an inlet of the heat exchanger 7 is communicated with an outlet of the second delivery pump 52, an outlet of the heat exchanger 7 is communicated with an inlet of the wastewater biochemical treatment system, and the pretreated wastewater 40 cooled to a certain temperature by heat exchange is discharged.
Further, when the temperature of the acidified wastewater entering the second transfer pump 52 is proper, heat exchange cooling through the heat exchanger 7 is not needed, a bypass liquid outlet pipeline 302 may be disposed on the second liquid outlet pipeline 301 communicated with the inlet of the heat exchanger 7, and the acidified wastewater mixed with the alkali solution 30 to a certain PH value is directly discharged through the bypass liquid outlet pipeline 302 by the second transfer pump 52. One end of the bypass liquid outlet pipeline 302 is communicated with the second liquid outlet pipeline 301, the other end of the bypass liquid outlet pipeline 302 is communicated with an inlet of the wastewater biochemical treatment system, and the wastewater 40 after the pretreatment after the PH adjustment is discharged to the wastewater biochemical treatment system for further treatment.
The wastewater treatment system provided by the embodiment of the invention has reasonable process, reduces the investment and arrangement of the storage tank and the pump, and reduces the construction cost; the Fenton reaction is changed into the acidification reaction, so that a large amount of cost is saved under the condition of the same pH value control, and the investment and operation cost is greatly reduced.
The above embodiments are only exemplary embodiments of the present invention, and are not intended to limit the present invention, and the scope of the present invention is defined by the claims. Various modifications and equivalents may be made by those skilled in the art within the spirit and scope of the present invention, and such modifications and equivalents should also be considered as falling within the scope of the present invention.
Claims (10)
1. A wastewater treatment system for pretreating wastewater from an oximation reaction, comprising:
the mixer is used for mixing the oximation stripping waste water with acid liquor;
the acidification reaction kettle is used for carrying out acidification reaction, and a discharge hole of the mixer is communicated with a first feed hole of the acidification reaction kettle;
the buffer tank is used for storing products after the acidification reaction, and a discharge hole of the acidification reaction kettle is communicated with an inlet of the buffer tank;
and the tail gas absorption tower is communicated with a first gas outlet of the acidification reaction kettle through a first gas outlet pipeline, and the gas inlet of the tail gas absorption tower is communicated with a second gas outlet of the buffer tank through a second gas outlet pipeline so as to absorb the acidification tail gas generated by the acidification reaction.
2. The wastewater treatment system of claim 1, further comprising a first return line, the first return line communicating the discharge port of the acidification reactor and a second feed port of the acidification reactor.
3. The wastewater treatment system of claim 2, wherein the discharge port of the acidification reaction kettle is communicated with the inlet of the buffer tank through a first liquid outlet pipe, the second feed port of the acidification reaction kettle is communicated with the first liquid outlet pipe through the first liquid return pipe, and a first delivery pump is arranged on the first liquid outlet pipe upstream of the first liquid return pipe.
4. The wastewater treatment system of claim 1, wherein the pH in the acidification reactor is 1.0 to 5.0, the temperature in the acidification reactor is 55 to 80 ℃, and the pressure in the acidification reactor is atmospheric pressure.
5. The wastewater treatment system of claim 1, further comprising a lye tank, wherein a lye outlet of the lye tank is in communication with an outlet of the surge tank via a lye line.
6. The wastewater treatment system of claim 5, wherein the outlet of the buffer tank is communicated with an inlet of a wastewater biochemical treatment system through a second liquid outlet pipe, a second delivery pump is arranged on the second liquid outlet pipe, and the alkaline liquid pipe is communicated with an inlet of the second delivery pump through the second liquid outlet pipe.
7. The wastewater treatment system of claim 6, further comprising a second return line disposed between the second effluent line downstream of the second transfer pump and the inlet of the lye tank for diluting the lye within the lye tank.
8. The wastewater treatment system of claim 7, further comprising a heat exchanger disposed on the second effluent line downstream of the second transfer pump.
9. The wastewater treatment system according to claim 5, wherein a third delivery pump is disposed on the lye pipeline near the lye outlet of the lye tank, a lye branch is connected between the lye pipeline and the liquid inlet of the tail gas absorption tower, and the third delivery pump is disposed upstream of the lye branch.
10. The wastewater treatment system of claim 1, wherein the tail gas absorption tower further comprises a liquid outlet disposed at the bottom of the tail gas absorption tower, the liquid outlet is communicated with an inlet of the buffer tank, and the liquid outlet is higher than the inlet of the buffer tank.
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| CN202010014305.3A CN111039339A (en) | 2020-01-07 | 2020-01-07 | Wastewater treatment system |
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| CN103951142A (en) * | 2014-05-13 | 2014-07-30 | 湖北三宁化工股份有限公司 | Treatment method and device for cyclohexanone ammoximation wastewater |
| CN205874093U (en) * | 2016-08-11 | 2017-01-11 | 湖北三宁化工股份有限公司 | Caprolactam waste water preprocessing device |
| CN208345928U (en) * | 2018-05-15 | 2019-01-08 | 湖北三宁化工股份有限公司 | The processing unit of cyclohexanone oxamidinating production technology exhaust gas |
| CN211644643U (en) * | 2020-01-07 | 2020-10-09 | 沧州旭阳化工有限公司 | Wastewater treatment system |
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2020
- 2020-01-07 CN CN202010014305.3A patent/CN111039339A/en not_active Withdrawn
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103951142A (en) * | 2014-05-13 | 2014-07-30 | 湖北三宁化工股份有限公司 | Treatment method and device for cyclohexanone ammoximation wastewater |
| CN205874093U (en) * | 2016-08-11 | 2017-01-11 | 湖北三宁化工股份有限公司 | Caprolactam waste water preprocessing device |
| CN208345928U (en) * | 2018-05-15 | 2019-01-08 | 湖北三宁化工股份有限公司 | The processing unit of cyclohexanone oxamidinating production technology exhaust gas |
| CN211644643U (en) * | 2020-01-07 | 2020-10-09 | 沧州旭阳化工有限公司 | Wastewater treatment system |
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Application publication date: 20200421 |