CN114314802A - Treatment device and method for organophosphorus wastewater from production of acephate - Google Patents
Treatment device and method for organophosphorus wastewater from production of acephate Download PDFInfo
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- CN114314802A CN114314802A CN202111551105.2A CN202111551105A CN114314802A CN 114314802 A CN114314802 A CN 114314802A CN 202111551105 A CN202111551105 A CN 202111551105A CN 114314802 A CN114314802 A CN 114314802A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 110
- 238000000034 method Methods 0.000 title claims abstract description 33
- YASYVMFAVPKPKE-UHFFFAOYSA-N acephate Chemical compound COP(=O)(SC)NC(C)=O YASYVMFAVPKPKE-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 9
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 313
- 239000007789 gas Substances 0.000 claims abstract description 64
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 53
- 239000011574 phosphorus Substances 0.000 claims abstract description 53
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 53
- 238000006243 chemical reaction Methods 0.000 claims abstract description 28
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000001301 oxygen Substances 0.000 claims abstract description 27
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 27
- 239000003054 catalyst Substances 0.000 claims abstract description 21
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 17
- 238000002360 preparation method Methods 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 16
- 238000002156 mixing Methods 0.000 claims description 66
- 239000007788 liquid Substances 0.000 claims description 28
- 238000001514 detection method Methods 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 238000012856 packing Methods 0.000 claims description 14
- 238000001179 sorption measurement Methods 0.000 claims description 14
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 12
- 229910001882 dioxygen Inorganic materials 0.000 claims description 12
- 238000001035 drying Methods 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 11
- 230000008569 process Effects 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 5
- 239000000945 filler Substances 0.000 claims description 3
- 230000003647 oxidation Effects 0.000 abstract description 7
- 238000005345 coagulation Methods 0.000 abstract description 2
- 230000015271 coagulation Effects 0.000 abstract description 2
- 238000012544 monitoring process Methods 0.000 abstract description 2
- 238000001556 precipitation Methods 0.000 abstract description 2
- 230000002195 synergetic effect Effects 0.000 abstract description 2
- 238000006555 catalytic reaction Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 238000007872 degassing Methods 0.000 description 2
- 239000002274 desiccant Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 230000021736 acetylation Effects 0.000 description 1
- 238000006640 acetylation reaction Methods 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 238000009360 aquaculture Methods 0.000 description 1
- 244000144974 aquaculture Species 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000009297 electrocoagulation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910000398 iron phosphate Inorganic materials 0.000 description 1
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- NNKVPIKMPCQWCG-UHFFFAOYSA-N methamidophos Chemical compound COP(N)(=O)SC NNKVPIKMPCQWCG-UHFFFAOYSA-N 0.000 description 1
- 239000003986 organophosphate insecticide Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000007146 photocatalysis Methods 0.000 description 1
- 230000001699 photocatalysis Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000008054 signal transmission Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
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Abstract
The invention provides a device and a method for treating organophosphorus wastewater from production of acephate, wherein the device comprises a wastewater reaction unit, an ozone preparation unit and an ozone recovery unit; the wastewater reaction unit and the ozone preparation unit improve the ozone solubility of the organophosphorus wastewater through pressurization and circulation setting, so as to improve the oxidation efficiency and the utilization rate of ozone, and oxidize and destroy phosphorus-containing organic matters in the organophosphorus wastewater for producing acephate under the synergistic action of a catalyst to convert the phosphorus-containing organic matters into inorganic phosphorus, wherein the converted inorganic phosphorus can be removed through various precipitation and coagulation modes; meanwhile, the incompletely reacted ozone and oxygen in the tail gas are secondarily utilized through the ozone recovery unit, so that the preparation cost of the ozone is reduced; the continuous and stable operation of the device is ensured and the safety of the device is ensured through the linkage of the monitoring equipment and the electromagnetic valve; the device and the method solve the problem of treatment of the organophosphorus wastewater for producing the acephate.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and relates to a device and a method for treating organophosphorus wastewater.
Background
Acephate, the common name acephate, is the acetylation product of methamidophos. Acephate is an organophosphorus insecticide widely used in the global scope and is one of large-tonnage pesticides in China. Various phosphorus-containing wastewater is generated in the production process of acephate products, meanwhile, individual wastewater also has the characteristics of high COD, high ammonia nitrogen and high salt, meanwhile, organic phosphorus is a pollutant which is difficult to remove in the field of wastewater treatment, organic phosphorus is generally required to be converted into inorganic phosphorus and then treated, but no particularly effective conversion method exists at present, so that the development of a targeted and high-economical treatment mode for the wastewater is urgent.
The method for treating wastewater by using ozone is a water treatment method widely used in the field of environmental protection at present, but due to the problems of low utilization rate of ozone, high energy consumption of an ozone generator and the like, many enterprises cannot bear the problem, for example, the concentration of ozone generally generated by an oxygen source ozone generator is only 10%, most of oxygen cannot be converted into ozone, and the ozone can only be wasted as tail gas emission. Meanwhile, the solubility of ozone in water is 26mg/L at normal pressure, and the solubility of ozone in water can be increased by 26mg/L whenever the pressure is increased by one atmosphere, so that the ozone reactor is generally fabricated as a cylindrical tower to increase the solubility of ozone, but the increase of the solubility is limited due to the height of the reactor.
The invention patent with publication number CN10618905 discloses an ozone-enhanced electrocoagulation treatment method for phosphorus-containing wastewater, which directly uses an iron electrode to treat the phosphorus-containing wastewater, and simultaneously adds ozone to partially oxidize phosphorus-containing organic substances and synchronously generate iron phosphate precipitate so as to remove phosphorus. The invention patent with the granted publication number of CN102328987B discloses an ozone reaction device, which realizes the treatment of aquaculture wastewater by the signal transmission of ORP electrodes and the dissolution of ozone by a jet device, but the device can not improve the utilization efficiency of ozone and can not effectively treat wastewater containing organic phosphorus. The invention patent with publication number CN110550804A discloses an industrial wastewater circulating treatment and purification device for ozone oxidation and a use method thereof, the method improves the oxidation performance of ozone by catalysis means such as ultrasonic waves, photocatalysis, electromagnetic catalysis and the like, but the method has high energy consumption and does not realize effective utilization of ozone. The patent publication No. CN111003860A discloses an apparatus for treating sludge wastewater with ozone and a using method thereof, wherein the method improves the oxidation capability and utilization efficiency of ozone through ultraviolet catalysis, but the method cannot treat wastewater containing organic phosphorus.
Disclosure of Invention
In order to solve the problems in the background art, the invention provides a device and a method for treating organophosphorus wastewater from acephate production.
A treatment device for organophosphorus wastewater from production of acephate comprises a wastewater reaction unit, an ozone preparation unit and an ozone recovery unit; the wastewater reaction unit comprises a high-pressure pump, a pressure-resistant circulating pump, an ejector and an ozone main reactor which are sequentially connected through pipelines, wherein the high-pressure pump is provided with an organophosphorus wastewater inlet, the ejector is connected with the lower inlet of the ozone main reactor through a pipeline, the middle upper part of the ozone main reactor is provided with a catalyst packing layer, and the upper part of the catalyst packing layer is provided with a water outlet pipeline; the ozone preparation unit comprises a third mixing valve, an ozone generator and an ozone compressor which are sequentially connected through a pipeline, the third mixing valve is provided with an oxygen inlet, and the ozone compressor is connected with an ejector of the wastewater reaction unit through a pipeline; the ozone recovery unit comprises a pressure reducing valve, a second ozone tail gas destructor, a first ozone tail gas destructor and a drying adsorption tower which are sequentially connected through a pipeline, wherein the pressure reducing valve is connected with a top outlet of an ozone main reactor of the wastewater reaction unit through a pipeline, and the drying adsorption tower is connected with a third mixing valve of the ozone preparation unit through a pipeline.
Furthermore, the wastewater reaction unit also comprises a mixing valve, the mixing valve is arranged between the high-pressure pump and the pressure-resistant circulating pump, and an inlet of the mixing valve is connected with a middle outlet of the ozone main reactor through a pipeline.
Furthermore, a liquid level sensor is arranged at the upper part of a catalyst packing layer in the ozone main reactor, a first electromagnetic valve is arranged on a water outlet pipeline of the ozone main reactor, and the opening and closing of the first electromagnetic valve are controlled by the liquid level sensor.
Furthermore, the top outlet of the ozone main reactor is connected with a pressure reducing valve through a second electromagnetic valve and a pipeline, the upper part of the ozone main reactor is provided with a first pressure sensor and a first ozone concentration detection sensor, and the opening and closing of the second electromagnetic valve are controlled through the first pressure sensor and the first ozone concentration detection sensor.
Further, the ozone preparation unit still includes No. two mixing valves, No. two mixing valves set up between the ejector of ozone compressor and waste water reaction unit, the import of No. two mixing valves still be connected through the side export on pipeline and ozone main reactor's level sensor upper portion.
Furthermore, the outlet of the first ozone tail gas destructor is provided with a third electromagnetic valve, the pipeline of the ozone recovery unit is provided with a second pressure sensor and a second ozone concentration detection sensor, and the opening and closing of the third electromagnetic valve are controlled by the second pressure sensor and the second ozone concentration detection sensor.
A method for treating organophosphorus wastewater from production of acephate comprises the following steps:
step one, the organophosphorus wastewater is collected to an ejector through a high-pressure pump, a first mixing valve and a pressure-resistant circulating pump;
step two, oxygen enters the ozone generator through the third mixing valve to react to generate ozone, and the ozone is subjected to pressure increase by the ozone compressor and then is collected to the ejector through the second mixing valve;
step three, mixing organic phosphorus wastewater and ozone, then entering the ozone main reactor from an inlet at the lower part of the ozone main reactor for carrying out ozone oxidation reaction, and discharging the wastewater after reaction through a first electromagnetic valve after flowing through a catalyst packing layer at the upper part of the ozone main reactor;
step four, the wastewater in the middle of the ozone main reactor enters the ejector again through a first mixing valve and a pressure-resistant circulating pump, the incompletely reacted ozone and oxygen in the upper part of the ozone main reactor enter the ejector again through a second mixing valve to be mixed with the organophosphorus wastewater, and the mixed ozone and oxygen enter the ozone main reactor to continue the ozone oxidation reaction;
and fifthly, enabling the mixture of the organic phosphorus wastewater and the ozone to fully react through the catalyst packing layer, and when the liquid level of the wastewater after the reaction reaches the liquid level sensor, enabling the first electromagnetic valve to be opened through a feedback signal of the liquid level sensor, and discharging the wastewater through the water outlet pipeline and the first electromagnetic valve.
Further, in the treatment process, when a pressure sensor arranged at the upper part of a liquid level sensor of the ozone main reactor monitors that the internal pressure of the ozone main reactor is higher than a limit value or an ozone concentration detection sensor monitors that the ozone concentration in a gas space is higher than the limit value, a second electromagnetic valve is opened, ozone and oxygen which are not completely reacted at the upper part of the ozone main reactor are discharged to a second ozone tail gas destructor and a first ozone tail gas destructor through a pressure reducing valve, the second ozone tail gas destructor and the first ozone tail gas destructor destroy residual ozone in tail gas to convert the residual ozone into oxygen gas, and the oxygen gas at the outlet of the first ozone tail gas destructor is dried by a drying adsorption tower and collected to an ozone generator E1 through a third mixing valve.
Further, in the treatment process, when a second pressure sensor arranged on a pipeline of the ozone recovery unit monitors that the pressure of the pipeline is higher than a limit value or a second ozone concentration detection sensor monitors that the ozone concentration of the pipeline is higher than the limit value, a third electromagnetic valve is opened, and the discharged gas is used for reducing the pressure of the pipeline.
Furthermore, the time for carrying out the ozone oxidation reaction on the organic phosphorus wastewater and the ozone mixture in the ozone main reactor R; the pressure in the sections among the outlet of the high-pressure pump, the outlet of the ozone compressor, the outlet of the second electromagnetic valve and the outlet of the first electromagnetic valve is less than or equal to 3.5 MPa; the pressure in the section between the outlet of the pressure reducing valve and the inlet of the ozone generator is less than or equal to 0.1 MPa.
In the waste water reaction unit, the high-pressure pump is used for providing organic phosphorus waste water to whole device and intakes, withstand voltage circulating pump is used for circulating the organic phosphorus waste water that has got into ozone main reactor, make the ozone that does not react completely dissolve with organic phosphorus waste water, and throw new ozone via the ejector, the ejector is used for carrying out ozone and organic phosphorus waste water and dissolves, the catalyst packing layer is used for promoting the oxidation efficiency of ozone, still play degasification's effect simultaneously, assemble into the gas space that big bubble shifted to catalyst packing layer upper portion with the tiny bubble of ozone and oxygen. In addition, the first electromagnetic valve is interlocked with the liquid level sensor, and the first electromagnetic valve is opened or closed through a feedback signal of the liquid level sensor to control water outlet; no. two solenoid valves are interlocked with a pressure sensor and an ozone concentration sensor simultaneously, and when the gas space pressure is too high or the gas space ozone concentration is too high, the solenoid valve discharge gas can be opened to reduce the pressure of the ozone main reactor in time, so that the safety of the device is ensured.
In the ozone preparation unit, an ozone generator and an ozone compressor are operated intermittently, the ozone generator is mainly used for preparing ozone, the ozone compressor is mainly used for pressurizing ozone gas so that the ozone can enter an ozone main reactor, and the ozone and oxygen which are not completely reacted at the upper part of the ozone main reactor enter an ejector through a second mixing valve again to be mixed with organic phosphorus wastewater and then enter the ozone main reactor for continuous reaction.
In the ozone recovery unit, the pressure reducing valve is mainly used for reducing the pressure of the tail gas conveyed by the ozone main reactor, the ozone tail gas destructor is mainly used for destroying residual ozone in the tail gas to convert the residual ozone into oxygen gas, and drying agents and adsorbents are filled in the drying adsorption tower respectively to remove moisture and a small amount of organic substances in the oxygen gas. In addition, the third electromagnetic valve is interlocked with the second pressure sensor and the second ozone concentration sensor, when the pressure in the section from the pressure reducing valve to the third mixing valve is too high or the ozone concentration is too high, the third electromagnetic valve is opened, and the released gas is used for reducing the pressure in the section so as to ensure the safety of the device.
Compared with the prior art, the ozone solubility of the organophosphorus wastewater is improved by the wastewater reaction unit and the ozone preparation unit through pressurization and circulation, so that the oxidation efficiency and the utilization rate of ozone are improved, under the synergistic effect of the catalyst, phosphorus-containing organic matters in the organophosphorus wastewater for producing acephate are oxidized and destroyed and converted into inorganic phosphorus, and the converted inorganic phosphorus can be removed through various precipitation and coagulation modes; the continuous and stable operation of the device is ensured and the safety of the device is ensured through the linkage of the monitoring equipment and the electromagnetic valve; the device and the method solve the problem of treatment of the organophosphorus wastewater for producing the acephate.
Drawings
FIG. 1 is a schematic view of an apparatus for treating organic phosphorus wastewater.
Wherein: r-ozone main reactor; e1-ozone generator; e2-ozone compressor; e3-ozone tail gas destroyer; e4-ozone tail gas destroyer; e5-jet device; p1-high pressure pump; p2-pressure resistant circulating pump; v1-solenoid valve number one; v2-solenoid valve No. two; v3-solenoid valve No. three; v4-mixing valve No. one; v5-mixing valve No. two; v6-mixing valve No. three; v7-pressure reducing valve; b1-pressure sensor No. one; b2-pressure sensor number two; (ii) a An L-level sensor; a1-ozone concentration detection sensor; a2-ozone concentration detection sensor No. two; a C-ozone catalyst; t-drying adsorption tower.
Detailed Description
The embodiments of the present invention will be described in detail with reference to the accompanying drawings, but the embodiments are not limited to the invention, and the advantages of the invention will be understood more clearly by the description. All modifications which can be derived or suggested by a person skilled in the art from the disclosure of the present invention are to be considered within the scope of the invention. The positional relationships described in the embodiments are all the same as those shown in the drawings, and other portions not described in detail in the embodiments are all the related art.
The device for treating organophosphorus wastewater shown in FIG. 1 comprises a wastewater reaction unit, an ozone preparation unit and an ozone recovery unit.
The wastewater reaction unit consists of a high-pressure pump P1, a first mixing valve V4, a pressure-resistant circulating pump P2, an ejector E5 and an ozone main reactor R. The high-pressure pump P1, the first mixing valve V4, the pressure-resistant circulating pump P2, the ejector E5 and the ozone main reactor R are connected in sequence through pipelines. The high-pressure pump P1 is provided with an organic phosphorus wastewater input port for providing organic phosphorus wastewater inlet water for the whole device; the ejector E5 is used for dissolving ozone and organic phosphorus wastewater, is connected with the inlet at the lower part of the ozone main reactor R through a pipeline, and conveys the mixture of the ozone and the organic phosphorus wastewater into the ozone main reactor R; the inlet of the first mixing valve V4 is also connected with the middle outlet of the ozone main reactor R through a pipeline, so that the mixture of the organic phosphorus wastewater and the ozone can be conveyed into a pressure-resistant circulating pump P2 again through the first mixing valve V4, the pressure-resistant circulating pump P2 is used for circulating the organic phosphorus wastewater entering the ozone main reactor R, the unreacted ozone and the organic phosphorus wastewater are dissolved, new ozone is added through the ejector E5, and the ejector E5 is used for dissolving the ozone and the organic phosphorus wastewater.
The middle upper part of the ozone main reactor R is provided with a catalyst packing layer C which is loaded with a metal inorganic catalyst and used for improving the oxidation efficiency of ozone, and simultaneously plays a role of degassing, so that tiny bubbles of ozone and oxygen are converged into large bubbles to be transferred to a gas space on the upper part of the catalyst packing layer C. The upper part of the catalyst packing layer C is provided with a liquid level sensor L and a water outlet pipeline, the water outlet pipeline is provided with a first electromagnetic valve V1, a first electromagnetic valve V1 is interlocked with the liquid level sensor L, and the first electromagnetic valve V1 is opened or closed through a feedback signal of the liquid level sensor L to control water outlet. The top outlet of the ozone main reactor R is connected with a pressure reducing valve V7 through a second electromagnetic valve V2 and a pipeline, the upper part of the liquid level sensor L is provided with a pressure sensor B1 and an ozone concentration detection sensor A1, the second electromagnetic valve V2 is interlocked with a pressure sensor B1 and an ozone concentration sensor A1, and when the pressure of a gas space is too high or the ozone concentration of the gas space is too high, the second electromagnetic valve V2 can be opened to discharge gas so as to reduce the pressure of the ozone main reactor R in time, so that the safety of the device is ensured.
The ozone preparation unit consists of a third mixing valve V6, an ozone generator E1, an ozone compressor E2 and a second mixing valve V5. The third mixing valve V6, the ozone generator E1, the ozone compressor E2 and the second mixing valve V5 are connected in sequence through pipelines. The third mixing valve V6 is provided with an oxygen inlet, the ozone generator E1 is used for preparing oxygen into ozone, the ozone is pressurized by the ozone compressor E2 and then is conveyed to the second mixing valve V5, the inlet of the second mixing valve V5 is also connected with the side outlet at the upper part of the liquid level sensor L of the ozone main reactor R through a pipeline, so that the ozone and the oxygen which are not completely reacted at the upper part of the ozone main reactor R can be conveyed to the second mixing valve V5, the ozone which is pressurized by the ozone compressor E2 and the ozone and the oxygen which are not completely reacted at the upper part of the ozone main reactor R are mixed in the second mixing valve V5, the mixed gas is conveyed to the ejector E5 and is mixed and dissolved with the organic phosphorus wastewater input in the ejector E5, and finally the mixture is conveyed to the ozone main reactor R for reaction.
The ozone recovery unit consists of a pressure reducing valve V7, a second ozone tail gas destructor E4, a first ozone tail gas destructor E3 and a drying adsorption tower T. The pressure reducing valve V7, the second ozone tail gas destructor E4, the first ozone tail gas destructor E3 and the drying adsorption tower T are sequentially connected through pipelines. The pressure reducing valve V7 is connected with the top outlet of the ozone main reactor R of the wastewater reaction unit through a pipeline and is used for reducing the pressure of the tail gas conveyed out of the ozone main reactor R; the second ozone tail gas destructor E4 and the first ozone tail gas destructor E3 destroy residual ozone in the tail gas to convert the residual ozone into oxygen gas; the drying and adsorption tower T is internally and respectively filled with a drying agent and an adsorbent, so that moisture and a small amount of organic substances in the oxygen gas can be removed, and the drying and adsorption tower T is connected with a third mixing valve V6 of the ozone preparation unit through a pipeline, so that the tail gas can be reused.
The outlet of the first ozone tail gas destructor E3 is provided with a third electromagnetic valve V3, a second pressure sensor B2 and a second ozone concentration detection sensor A2 are arranged on the pipeline of the ozone recovery unit, the third electromagnetic valve V3 is interlocked with the second pressure sensor B2 and the second ozone concentration sensor A2 at the same time, when the pressure in the section from the pressure reducing valve V7 to the third mixing valve V6 is too high or the ozone concentration is too high, the third electromagnetic valve V3 is opened, and the section is depressurized by the relief gas so as to ensure the safety of the device.
A method for treating organophosphorus wastewater from production of acephate comprises the following steps:
step one, the organic phosphorus wastewater is collected to an ejector E5 through a high-pressure pump P1, a first mixing valve V4 and a pressure-resistant circulating pump P2,
step two, oxygen enters an ozone generator E1 through a third mixing valve V6 to react to generate ozone, and the ozone is also converged to an ejector E5 through a second mixing valve V5 after the pressure of the ozone is increased by an ozone compressor E2;
step three, mixing organic phosphorus wastewater and ozone in an ejector, and then entering the ozone main reactor R from an inlet at the lower part of the ozone main reactor R to perform ozone oxidation reaction;
step four, the wastewater in the middle of the ozone main reactor R enters the ejector E5 again through the first mixing valve V4 and the pressure-resistant circulating pump P2, the incompletely reacted ozone and oxygen in the upper part of the ozone main reactor R enter the ejector E5 again through the second mixing valve V5 to be mixed with the organic phosphorus wastewater, and the mixed wastewater enters the ozone main reactor R to continue the ozone oxidation reaction;
and step five, enabling the mixture of the organic phosphorus wastewater and the ozone to fully react through the catalyst filler layer C, enabling the first electromagnetic valve V1 to be opened through a feedback signal of the liquid level sensor L when the liquid level of the wastewater after the reaction reaches the liquid level sensor L, and discharging the wastewater through a water outlet pipeline and the first electromagnetic valve V1.
The section between the outlet of a high-pressure pump P1, the outlet of an ozone compressor E2, the outlet of a second electromagnetic valve V2 and the outlet of a first electromagnetic valve V1 is a high-pressure part of the device, the pressure in the section is less than or equal to 3.5MPa, and the section between the outlet of a pressure reducing valve V7 and the inlet of an ozone generator E1 is a low-pressure part of the device, and the pressure in the section is less than or equal to 0.1 MPa.
In the treatment process, when a first pressure sensor B1 arranged at the upper part of a liquid level sensor L of an ozone main reactor R monitors that the internal pressure of the ozone main reactor R is higher than a limit value or a first ozone concentration detection sensor A1 monitors that the ozone concentration in a gas space is higher than the limit value, a second electromagnetic valve V2 is opened, ozone and oxygen which are not completely reacted at the upper part of the ozone main reactor R are discharged into a second ozone tail gas destructor E4 and a first ozone tail gas destructor E3 through a pressure reducing valve V7, residual ozone in tail gas is destroyed by the second ozone tail gas destructor E4 and the first ozone tail gas destructor E3 to be converted into oxygen gas, and the oxygen gas at the outlet of the first ozone tail gas destructor E3 is dried through a drying adsorption tower T and then collected into an ozone generator E1 through a third mixing valve V6.
In the treatment process, when a second pressure sensor B2 arranged on a pipeline of the ozone recovery unit monitors that the pressure of the pipeline is higher than a limit value or a second ozone concentration detection sensor A2 monitors that the ozone concentration of the pipeline is higher than the limit value, a third electromagnetic valve V3 is opened, and the exhaust gas is used for depressurizing the pipeline.
Examples
The water quality of organophosphorus wastewater for producing acephate is as follows: 4000mg/L of organic phosphorus, 35mg/L of inorganic phosphorus, 13000mg/L of COD, 5 percent of salt and 9.0 of pH, and the organic phosphorus wastewater is treated by applying the treatment device and the treatment method.
(1) The pressure in the high-pressure section of the control device is 3Mpa, the residence reaction time of the mixture of the organophosphorus wastewater and the ozone in the ozone main reactor R is 2.5h, the pressure in the low-pressure section of the control device is 0.1Mpa, the mixing proportion is adjusted to be 50% by all mixing valves, and the ozone adding amount is controlled to be 20000 mg/L.
(2) The organic phosphorus wastewater is imported into a first mixing valve V4 through a high-pressure pump P1, flows through a pressure-resistant circulating pump P2 and is imported into an ejector E5; oxygen enters the ozone generator E1 through a third mixing valve V6 to react to generate ozone, and the ozone is pressurized by the ozone compressor E2 and then is collected to the ejector E5 through a second mixing valve V5.
(3) The organic phosphorus wastewater and ozone are fully mixed at the E5 position of the ejector, and then enter the main ozone reactor R for carrying out ozone oxidation reaction, meanwhile, the wastewater in the middle of the main ozone reactor R enters the ejector E5 again through the first mixing valve V4 and the pressure-resistant circulating pump P2, the ozone and oxygen which are not completely reacted at the upper part of the main ozone reactor R enter the ejector E5 again through the second mixing valve V5 to be mixed with the organic phosphorus wastewater, and the mixed wastewater enters the main ozone reactor R for continuing the ozone oxidation reaction; the solubility of ozone in the ozone main reactor R can reach more than 500mg/L, and the mixture of the organophosphorus wastewater and the ozone fully reacts under the catalytic action of a catalyst packing layer C.
(4) When the liquid level of the reacted wastewater reaches the liquid level sensor L, the first electromagnetic valve V1 is opened through the feedback signal of the liquid level sensor L, and the wastewater is discharged through the water outlet pipeline and the first electromagnetic valve V1.
In the treatment process, when a first pressure sensor B1 arranged at the upper part of a liquid level sensor L of an ozone main reactor R monitors that the internal pressure of the ozone main reactor R is higher than a limit value or a first ozone concentration detection sensor A1 monitors that the ozone concentration in a gas space is higher than the limit value, a second electromagnetic valve V2 is opened, ozone and oxygen which are not completely reacted at the upper part of the ozone main reactor R are discharged to a second ozone tail gas destructor E4 and a first ozone tail gas destructor E3 through a pressure reducing valve V7, the oxygen gas at the outlet of the first ozone tail gas destructor E3 is dried through a drying adsorption tower T and then is collected into an ozone generator E1 through a third mixing valve V6, and the recovered oxygen gas and fresh oxygen are mixed and enter an ozone generator E1 to prepare ozone. When a second pressure sensor B2 arranged on a pipeline of the ozone recovery unit monitors that the pressure of the pipeline is higher than a limit value or a second ozone concentration detection sensor A2 monitors that the ozone concentration of the pipeline is higher than the limit value, a third electromagnetic valve V3 is opened, and the exhausted gas is used for reducing the pressure of the pipeline.
The water quality of the treated organophosphorus wastewater for producing the acephate is as follows: 5mg/L of organic phosphorus, 4030mg/L of inorganic phosphorus, 5000mg/L of COD, 5 percent of salt and 7.0 of pH. After treatment, organic phosphorus in the wastewater is effectively removed, and the COD index is greatly reduced.
The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings and specific examples, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
Claims (10)
1. The utility model provides a processing apparatus of organophosphorus waste water of production acephate which characterized in that: comprises a wastewater reaction unit, an ozone preparation unit and an ozone recovery unit;
the wastewater reaction unit comprises a high-pressure pump (P1), a pressure-resistant circulating pump (P2), an ejector (E5) and a main ozone reactor (R) which are sequentially connected through pipelines, wherein the high-pressure pump (P1) is provided with an organic phosphorus wastewater inlet, the ejector (E5) is connected with an inlet at the lower part of the main ozone reactor (R) through a pipeline, a catalyst packing layer (C) is arranged at the middle upper part of the main ozone reactor (R), and a water outlet pipeline is arranged at the upper part of the catalyst packing layer (C);
the ozone preparation unit comprises a third mixing valve (V6), an ozone generator (E1) and an ozone compressor (E2) which are sequentially connected through a pipeline, the third mixing valve (V6) is provided with an oxygen inlet, and the ozone compressor (E2) is connected with an ejector (E5) of the wastewater reaction unit through a pipeline;
ozone recovery unit include relief pressure valve (V7), No. two ozone tail gas destroys ware (E4), No. one ozone tail gas destroys ware (E3) and dry adsorption tower (T) that connect gradually through the pipeline, relief pressure valve (V7) link to each other through the top export of the ozone main reactor (R) of pipeline with waste water reaction unit, dry adsorption tower (T) be connected through pipeline and ozone preparation unit's No. three blend valve (V6).
2. The device for treating organophosphorus wastewater for producing acephate according to claim 1, wherein: the wastewater reaction unit also comprises a first mixing valve (V4), the first mixing valve (V4) is arranged between the high-pressure pump (P1) and the pressure-resistant circulating pump (P2), and the inlet of the first mixing valve (V4) is connected with the middle outlet of the ozone main reactor (R) through a pipeline.
3. The apparatus for treating organophosphorus wastewater for producing acephate according to claim 1 or 2, wherein: the upper part of a catalyst packing layer (C) in the ozone main reactor (R) is provided with a liquid level sensor (L), a water outlet pipeline of the ozone main reactor (R) is provided with a first electromagnetic valve (V1), and the opening and closing of the first electromagnetic valve (V1) are controlled by the liquid level sensor (L).
4. The device for treating organophosphorus wastewater for producing acephate according to claim 3, wherein: the top outlet of the ozone main reactor (R) is connected with a pressure reducing valve (V7) through a second electromagnetic valve (V2) and a pipeline, the upper part of the ozone main reactor (R) is provided with a pressure sensor (B1) and an ozone concentration detection sensor (A1), and the opening and closing of the second electromagnetic valve (V2) are controlled through the first pressure sensor (B1) and the first ozone concentration detection sensor (A1).
5. The device for treating organophosphorus wastewater for producing acephate according to claim 4, wherein: the ozone preparation unit also comprises a second mixing valve (V5), the second mixing valve (V5) is arranged between the ozone compressor (E2) and the ejector (E5) of the wastewater reaction unit, and the inlet of the second mixing valve (V5) is also connected with the side outlet at the upper part of the liquid level sensor (L) of the ozone main reactor (R) through a pipeline.
6. The apparatus for treating organophosphorus wastewater for producing acephate according to claim 1, 3 or 5, wherein: the export of a ozone tail gas destructor (E3) be provided with No. three solenoid valves (V3), ozone recovery unit's pipeline on be provided with No. two pressure sensor (B2) and No. two ozone concentration detection sensor (A2), the opening and close of No. three solenoid valve (V3) control through No. two pressure sensor (B2) and No. two ozone concentration detection sensor (A2).
7. A treatment method of organophosphorus wastewater for producing acephate is characterized by comprising the following steps:
firstly, organic phosphorus wastewater is collected to an ejector (E5) through a high-pressure pump (P1), a first mixing valve (V4) and a pressure-resistant circulating pump (P2);
step two, oxygen enters an ozone generator (E1) through a third mixing valve (V6) to react to generate ozone, and the ozone is subjected to pressure increase through an ozone compressor (E2) and then is collected to an ejector (E5) through a second mixing valve (V5);
step three, mixing organic phosphorus wastewater and ozone, then entering the ozone main reactor (R) from an inlet at the lower part of the ozone main reactor (R) for carrying out ozone oxidation reaction, and discharging the wastewater after the reaction through a first electromagnetic valve (V1) after flowing through a catalyst filler layer (C) at the upper part of the ozone main reactor (R);
step four, the wastewater in the middle of the ozone main reactor (R) enters the ejector (E5) again through a first mixing valve (V4) and a pressure-resistant circulating pump (P2), the incompletely reacted ozone and oxygen on the upper part of the ozone main reactor (R) enter the ejector (E5) again through a second mixing valve (V5) to be mixed with the organophosphorus wastewater, and the mixed ozone and oxygen enter the ozone main reactor (R) to continue the ozone oxidation reaction;
and fifthly, enabling the mixture of the organic phosphorus wastewater and the ozone to fully react through the catalyst filler layer C, enabling the first electromagnetic valve (V1) to be opened through a feedback signal of the liquid level sensor (L) when the liquid level of the wastewater after the reaction reaches the liquid level sensor (L), and discharging the wastewater through a water outlet pipeline and the first electromagnetic valve (V1).
8. The method for treating organophosphorus wastewater for producing acephate according to claim 7, wherein the method comprises the following steps: in the treatment process, when a first pressure sensor (B1) arranged at the upper part of a liquid level sensor (L) of an ozone main reactor (R) monitors that the internal pressure of the ozone main reactor (R) is higher than a limit value or a first ozone concentration detection sensor (A1) monitors that the ozone concentration in a gas space is higher than the limit value, the second electromagnetic valve (V2) is opened, ozone and oxygen which are not completely reacted at the upper part of the ozone main reactor (R) are discharged to the second ozone tail gas destructor (E4) and the first ozone tail gas destructor (E3) through a pressure reducing valve (V7), residual ozone in the tail gas is destroyed by the second ozone tail gas destructor (E4) and the first ozone tail gas destructor (E3) to be converted into oxygen gas, and the oxygen gas at the outlet of the first ozone tail gas destructor (E3) is dried by a drying adsorption tower T and then is collected into an ozone generator (E1) through a third mixing valve (V6).
9. The method for treating organophosphorus wastewater for producing acephate according to claim 8, wherein the method comprises the following steps: in the treatment process, when a second pressure sensor (B2) arranged on a pipeline of the ozone recovery unit monitors that the pressure of the pipeline is higher than a limit value or a second ozone concentration detection sensor (A2) monitors that the ozone concentration of the pipeline is higher than the limit value, a third electromagnetic valve (V3) is opened, and the exhaust gas is used for depressurizing the pipeline.
10. The method for treating organophosphorus wastewater for producing acephate according to any one of claims 7 to 9, wherein: the time of carrying out ozone oxidation reaction on the organic phosphorus wastewater and the ozone mixture in the ozone main reactor (R) is more than or equal to 2 hours; the pressure in the section between the outlet of the high-pressure pump (P1), the outlet of the ozone compressor (E2), the outlet of the second electromagnetic valve (V2) and the outlet of the first electromagnetic valve (V1) is less than or equal to 3.5 MPa; the pressure in the section between the outlet of the pressure reducing valve (V7) and the inlet of the ozone generator (E1) is less than or equal to 0.1 MPa.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013000115A1 (en) * | 2011-06-28 | 2013-01-03 | Linde Aktiengesellschaft | Ozone treatment of wastewater |
| CN112225380A (en) * | 2020-10-19 | 2021-01-15 | 南通醋酸纤维有限公司 | Resource intensive phosphorus-containing wastewater treatment method |
| CN212894223U (en) * | 2020-07-07 | 2021-04-06 | 北京宜清源科技有限公司 | Processing system of oily phosphorus-containing high COD auto-parts cleaning wastewater |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013000115A1 (en) * | 2011-06-28 | 2013-01-03 | Linde Aktiengesellschaft | Ozone treatment of wastewater |
| CN212894223U (en) * | 2020-07-07 | 2021-04-06 | 北京宜清源科技有限公司 | Processing system of oily phosphorus-containing high COD auto-parts cleaning wastewater |
| CN112225380A (en) * | 2020-10-19 | 2021-01-15 | 南通醋酸纤维有限公司 | Resource intensive phosphorus-containing wastewater treatment method |
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