CN114314802B - Device and method for treating organophosphorus wastewater from production of acephate - Google Patents
Device and method for treating organophosphorus wastewater from production of acephate Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 110
- 238000000034 method Methods 0.000 title claims abstract description 37
- YASYVMFAVPKPKE-UHFFFAOYSA-N acephate Chemical compound COP(=O)(SC)NC(C)=O YASYVMFAVPKPKE-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 title abstract description 7
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 322
- 239000007789 gas Substances 0.000 claims abstract description 65
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 40
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 40
- 239000011574 phosphorus Substances 0.000 claims abstract description 40
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000001301 oxygen Substances 0.000 claims abstract description 24
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 239000003054 catalyst Substances 0.000 claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 20
- 238000002360 preparation method Methods 0.000 claims abstract description 17
- 238000011084 recovery Methods 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims description 65
- 239000007788 liquid Substances 0.000 claims description 27
- 238000001514 detection method Methods 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 238000001035 drying Methods 0.000 claims description 15
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 13
- 229910001882 dioxygen Inorganic materials 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 12
- 238000001179 sorption measurement Methods 0.000 claims description 12
- 239000000945 filler Substances 0.000 claims description 11
- 238000012856 packing Methods 0.000 claims description 7
- 238000004065 wastewater treatment Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 abstract description 8
- 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
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 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
- 239000005955 Ferric phosphate Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 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
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 229940032958 ferric phosphate Drugs 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000010842 industrial wastewater Substances 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
- 229910000399 iron(III) phosphate Inorganic materials 0.000 description 1
- 239000002184 metal Substances 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
- 238000000746 purification Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention provides a device and a method for treating organophosphorus wastewater for producing 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 are arranged in a pressurizing and circulating way to improve the ozone solubility of the organophosphorus wastewater, further improve the oxidation efficiency and the utilization rate of ozone, oxidize and destroy phosphorus-containing organic matters in the organophosphorus wastewater for producing acephate under the synergistic effect of a catalyst, convert the phosphorus-containing organic matters into inorganic phosphorus, and remove the converted inorganic phosphorus in various precipitation and coagulation modes; meanwhile, the ozone recovery unit secondarily utilizes the ozone and oxygen which are not completely reacted in the tail gas, so that the preparation cost of the ozone is reduced; the continuous and stable operation of the device is ensured by the linkage of the monitoring equipment and the electromagnetic valve, and the safety of the device is ensured; the device and the method solve the problem of disposal of the organophosphorus wastewater in the production of acephate.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and relates to an organic phosphorus wastewater treatment device and method.
Background
Acephate, commonly known as acephate, is the acetylated product of methamidophos. Acephate is an organophosphorus insecticide widely used in the global scope and is also one of large-tonnage pesticide varieties 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 type of pollutant which is difficult to remove in the field of wastewater treatment, and the organic phosphorus is usually 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 of the wastewater is urgent.
The wastewater treatment by utilizing ozone is a widely used water treatment method in the current environmental protection field, but due to the low utilization rate of ozone, high energy consumption of an ozone generator and other problems, many enterprises cannot bear the wastewater treatment method, for example, the concentration of ozone commonly generated by an oxygen source ozone generator is only 10%, and most of oxygen cannot be converted into ozone and can only be wasted as tail gas emission. Meanwhile, at normal pressure, the solubility of ozone in water is 26mg/L, and every time the pressure is increased by one atmosphere, the solubility of ozone in water can be increased by 26mg/L, so that the ozone reactor is usually manufactured as a cylindrical tower to improve the solubility of ozone, but the improvement of the solubility is limited by the height of the reactor.
The invention patent with publication number of CN10618905 discloses an ozone-enhanced electroflocculation treatment method for phosphorus-containing wastewater, which is characterized in that the method is characterized in that the phosphorus-containing wastewater is directly treated by using a ferroelectric, and ozone is added, so that phosphorus-containing organic substances can be partially oxidized, ferric phosphate precipitates are synchronously generated, and further phosphorus is removed, but the method has limited oxidation efficiency, and hydrogen is generated by a cathode in the treatment process, so that potential safety hazards are caused. The invention patent with publication number CN102328987B discloses an ozone reaction device, which dissolves ozone through ORP electrode signal conduction and further realizes the treatment of aquaculture wastewater by an ejector, 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 of CN110550804A discloses an industrial wastewater recycling treatment purification device for ozone oxidation and a use method thereof, wherein the method improves the oxidation performance of ozone by catalytic means such as ultrasonic wave, photocatalysis, electromagnetic catalysis and the like, but the method has higher energy consumption and does not realize the effective utilization of ozone. The invention patent with publication number of CN111003860A discloses equipment for treating sludge and wastewater by ozone and a using method thereof, wherein the method improves the oxidation capacity and the utilization efficiency of the ozone by ultraviolet catalysis, but the method cannot treat wastewater containing organic phosphorus.
Disclosure of Invention
In order to solve the problems in the background technology, the invention provides a device and a method for treating organophosphorus wastewater for producing acephate.
An organic phosphorus wastewater treatment device for producing 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 a pipeline, wherein the high-pressure pump is provided with an organophosphorus wastewater input port, the ejector is connected with the lower inlet of the ozone main reactor through the pipeline, the middle upper part of the ozone main reactor is provided with a catalyst filler layer, and the upper part of the catalyst filler 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, wherein 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 pipelines, wherein the pressure reducing valve is connected with the top outlet of the 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.
Further, the waste water reaction unit also comprises a first mixing valve, the first mixing valve is arranged between the high-pressure pump and the pressure-resistant circulating pump, and an inlet of the first mixing valve is connected with a middle outlet of the ozone main reactor through a pipeline.
Further, a liquid level sensor is arranged at the upper part of the catalyst filler 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.
Further, the top outlet of the ozone main reactor is connected with the pressure reducing valve through a second electromagnetic valve and a pipeline, a first pressure sensor and a first ozone concentration detection sensor are arranged on the upper portion of the ozone main reactor, and the opening and closing of the second electromagnetic valve is controlled through the first pressure sensor and the first ozone concentration detection sensor.
Further, the ozone preparation unit also comprises a second mixing valve, the second mixing valve is arranged between the ozone compressor and the ejector of the wastewater reaction unit, and the inlet of the second mixing valve is also connected with the side outlet at the upper part of the liquid level sensor of the ozone main reactor through a pipeline.
Furthermore, an outlet of the first ozone tail gas destructor is provided with a third electromagnetic valve, a 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 is controlled through the second pressure sensor and the second ozone concentration detection sensor.
A method for treating organophosphorus wastewater from acephate production comprises the following steps:
step one, the organophosphorus wastewater is converged to an ejector through a high-pressure pump, a first mixing valve and a pressure-resistant circulating pump;
step two, oxygen enters an ozone generator through a mixing valve III to react to generate ozone, and the ozone is converged to an ejector through a mixing valve II after the pressure of the ozone is increased through an ozone compressor;
step three, after the organic phosphorus wastewater and ozone are mixed, the mixed wastewater enters the ozone main reactor from the inlet at the lower part of the ozone main reactor to carry out ozone oxidation reaction, and the reacted wastewater flows through the catalyst packing layer at the upper part of the ozone main reactor and is discharged through a first electromagnetic valve;
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, and the ozone and oxygen which are not fully reacted 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 enter the ozone main reactor to continuously perform ozone oxidation reaction after being mixed;
and fifthly, fully reacting the mixture of the organophosphorus wastewater and the ozone through the catalyst filler layer, and when the liquid level of the reacted wastewater reaches the position of the liquid level sensor, opening the first electromagnetic valve through a feedback signal of the liquid level sensor, and discharging the wastewater through a water outlet pipeline and the first electromagnetic valve.
Further, in the treatment process, when the first pressure sensor arranged on the upper part of the liquid level sensor of the ozone main reactor monitors that the internal pressure of the ozone main reactor is higher than the limit value or the first ozone concentration detection sensor monitors that the ozone concentration of the gas space is higher than the limit value, the second electromagnetic valve is opened, ozone and oxygen which are not fully reacted on the upper part of the ozone main reactor are discharged to the second ozone tail gas destructor and the first ozone tail gas destructor through the pressure reducing valve, the second ozone tail gas destructor and the first ozone tail gas destructor destroy residual ozone in tail gas to be converted into oxygen gas, and the oxygen gas at the outlet of the first ozone tail gas destructor is collected into the ozone generator E1 through the third mixing valve after being dried through the drying adsorption tower.
Further, in the treatment process, when the second pressure sensor arranged on the pipeline of the ozone recovery unit monitors that the pipeline pressure is higher than the limit value or the second ozone concentration detection sensor monitors that the ozone concentration of the pipeline is higher than the limit value, the third electromagnetic valve is opened, and the pressure of the discharged gas is reduced to the pipeline.
Further, the time for the mixture of the organophosphorus wastewater and the ozone to undergo ozone oxidation reaction in the ozone main reactor R; the pressure in the section between the outlet of the high-pressure pump and the outlet of the ozone compressor and the outlets of the second electromagnetic valve and the first electromagnetic valve is less than or equal to 3.5MPa; 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 0.1MPa.
In the wastewater reaction unit, a high-pressure pump is used for supplying water to the whole device, a pressure-resistant circulating pump is used for circulating the organophosphorus wastewater which enters the ozone main reactor, so that the unreacted complete ozone and the organophosphorus wastewater are dissolved, new ozone is added through an ejector, the ejector is used for dissolving the ozone and the organophosphorus wastewater, a catalyst packing layer is used for improving the oxidation efficiency of the ozone, and meanwhile, the high-pressure circulating pump also has a degassing effect, and tiny bubbles of the ozone and oxygen are converged into big bubbles and transferred to a gas space at the upper part of the catalyst packing layer. 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; the second electromagnetic valve is simultaneously interlocked with the first pressure sensor and the first ozone concentration sensor, and when the gas space pressure is too high or the gas space ozone concentration is too high, the second electromagnetic valve can be opened to discharge gas, and the pressure of the ozone main reactor is timely reduced, 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 main purpose of the ozone generator is to prepare ozone, the main purpose of the ozone compressor is to pressurize ozone gas, so that ozone can enter an ozone main reactor, and ozone and oxygen which are not reacted completely at the upper part of the ozone main reactor enter an ejector again through a second mixing valve to be mixed with organophosphorus wastewater and then enter the ozone main reactor to continue to react.
In the ozone recovery unit, the main purpose of the pressure reducing valve is to reduce the pressure of the tail gas conveyed by the ozone main reactor, and the ozone tail gas destructor is mainly used for destroying the residual ozone in the tail gas to convert the residual ozone into oxygen gas, and the drying adsorption tower is internally filled with a drying agent and an adsorbent respectively, so that the moisture and a small amount of organic substances in the oxygen gas can be removed. In addition, the third electromagnetic valve is simultaneously 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 pressure of the section is reduced by the release gas so as to ensure the safety of the device.
Compared with the prior art, the wastewater reaction unit and the ozone preparation unit are arranged in a pressurizing and circulating way, so that the ozone solubility of the organophosphorus wastewater is improved, the oxidation efficiency and the utilization rate of ozone are further improved, under the synergistic effect of a catalyst, phosphorus-containing organic matters in the organophosphorus wastewater for producing acephate are oxidized and destroyed, the phosphorus-containing organic matters are converted into inorganic phosphorus, the converted inorganic phosphorus can be removed in various precipitation and coagulation modes, and the device and the method can achieve the conversion rate of the organic phosphorus in the organophosphorus wastewater for producing the acephate to more than 98%, and simultaneously the ozone and oxygen which are not fully reacted in tail gas are secondarily utilized by the ozone recovery unit, so that the preparation cost of the ozone is reduced; the continuous and stable operation of the device is ensured by the linkage of the monitoring equipment and the electromagnetic valve, and the safety of the device is ensured; the device and the method solve the problem of disposal of the organophosphorus wastewater in the production of acephate.
Drawings
FIG. 1 is a schematic view of an apparatus for treating organophosphorus wastewater.
Wherein: an R-ozone main reactor; e1-an ozone generator; e2-an ozone compressor; e3-an ozone tail gas destructor; E4-No. two ozone tail gas destructors; e5-jet means; p1-a high-pressure pump; p2-a pressure-resistant circulating pump; v1-solenoid valve number one; v2-solenoid valve number two; v3-solenoid valve III; v4-mixing valve number one; v5-mixing valve II; v6-mixing valve III; v7-a pressure reducing valve; b1-pressure sensor number one; b2-pressure sensor number two; an L-level sensor; a1-an ozone concentration detection sensor; a2-ozone concentration detection sensor; a C-ozone catalyst; t-drying adsorption tower.
Detailed Description
The following detailed description of the invention, taken in conjunction with the accompanying drawings, is not intended to limit the invention, but is made merely by way of example, and the advantages of the invention will be more clearly understood. All modifications directly derived or suggested to one skilled in the art from the disclosure of the present invention should be considered as being within the scope of the present invention. The positional relationship described in the embodiments is the same as that shown in the drawings, and other parts not described in detail in the embodiments are all prior art.
The device for treating the 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 sequentially connected through pipelines. The high-pressure pump P1 is provided with an organophosphorus wastewater input port for supplying organophosphorus wastewater to the whole device; the ejector E5 is used for dissolving ozone and organophosphorus wastewater, is connected with the inlet at the lower part of the ozone main reactor R through a pipeline, and is used for conveying the mixture of the ozone and the organophosphorus 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 the 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 which enters the ozone main reactor R, the unreacted complete 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 filler layer C, and the catalyst filler layer C is loaded with a metal inorganic catalyst for improving the oxidation efficiency of ozone, and simultaneously has the function of degassing, so that tiny bubbles of ozone and oxygen are converged into big bubbles and transferred to a gas space at the upper part of the catalyst filler layer C. The upper portion of catalyst packing layer C is provided with liquid level sensor L and water outlet pipeline, is provided with solenoid valve V1 No. one on the water outlet pipeline, and solenoid valve V1 is interlocked with liquid level sensor L, opens or closes solenoid valve V1 No. one through liquid level sensor L's feedback signal, controls the play water. 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, a first pressure sensor B1 and a first ozone concentration detection sensor A1 are arranged on the upper portion of the liquid level sensor L, the second electromagnetic valve V2 is simultaneously interlocked with the first pressure sensor B1 and the first ozone concentration sensor A1, and when the gas space pressure is too high or the gas space ozone concentration is too high, the second electromagnetic valve V2 can be opened to discharge gas and timely reduce the pressure of the ozone main reactor R so as to ensure the safety of the device.
The ozone preparation unit is composed 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 sequentially connected through pipelines. The third mixing valve V6 is provided with an oxygen inlet, the ozone generator E1 is used for preparing the 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 a 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 fully reacted at the upper part of the ozone main reactor R can be conveyed to the second mixing valve V5, the ozone and the ozone which are not fully reacted at the upper part of the ozone main reactor R after being pressurized by the ozone compressor E2 are mixed in the second mixing valve V5, the mixed gas is conveyed to the jet device E5 to be mixed and dissolved with the organophosphorus wastewater which is input into the jet device E5, and finally the mixture is conveyed to the ozone main reactor R for reaction.
The ozone recovery unit is composed 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 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, so that the residual ozone is converted into oxygen gas; the drying and adsorbing tower T is internally filled with a drying agent and an adsorbent respectively, so that moisture and a small amount of organic substances in oxygen gas can be removed, and the drying and adsorbing tower T is connected with a third mixing valve V6 of the ozone preparation unit through a pipeline, so that tail gas can be reused.
The export of ozone tail gas destructor E3 is provided with No. three solenoid valve V3, be provided with No. two pressure sensor B2 and No. two ozone concentration detection sensor A2 on ozone recovery unit's the pipeline, no. three solenoid valve V3 links with No. two pressure sensor B2 and No. two ozone concentration sensor A2 simultaneously, when pressure in relief pressure valve V7 to No. three mixing valve V6 district section is too high or ozone concentration is too high, then open No. three solenoid valve V3, the relief gas steps down this district section to guarantee the security of device.
A method for treating organophosphorus wastewater from acephate production comprises the following steps:
step one, the organophosphorus wastewater is converged into 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 mixing valve V6 to react to generate ozone, and the ozone is pressurized by an ozone compressor E2 and then is converged to an ejector E5 through a mixing valve V5;
step three, after the organic phosphorus wastewater and ozone are mixed in an ejector, the mixture enters an ozone main reactor R from the lower inlet of the ozone main reactor R for 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 ozone and oxygen which are not fully reacted 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 organophosphorus wastewater, and the mixed wastewater enters the ozone main reactor R to continue to carry out ozone oxidation reaction;
and fifthly, fully reacting the mixture of the organophosphorus wastewater and the ozone through the catalyst filler layer C, and when the liquid level of the reacted wastewater reaches the position of the liquid level sensor L, opening the first electromagnetic valve V1 through a feedback signal of the liquid level sensor L, and discharging the wastewater through a water outlet pipeline and the first electromagnetic valve V1.
The organic phosphorus wastewater and ozone mixture is subjected to ozone oxidation reaction in an ozone main reactor (the time of ozone oxidation reaction is more than or equal to 2 hours; 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 0.1MPa.
In the treatment process, when the pressure sensor B1 arranged at the upper part of the liquid level sensor L of the ozone main reactor R monitors that the internal pressure of the ozone main reactor R is higher than the limit value or the ozone concentration detection sensor A1 monitors that the ozone concentration of the gas space is higher than the limit value, the electromagnetic valve V2 is opened, ozone and oxygen which are not fully reacted at the upper part of the ozone main reactor R are discharged into the ozone tail gas destructor E4 and the ozone tail gas destructor E3 through the pressure reducing valve V7, residual ozone in the tail gas is destroyed by the ozone tail gas destructor E4 and the ozone tail gas destructor E3 to be converted into oxygen gas, and the oxygen gas at the outlet of the ozone tail gas destructor E3 is collected into the ozone generator E1 through the mixing valve V6 after being dried through the drying adsorption tower T.
In the treatment process, when the second pressure sensor B2 arranged on the pipeline of the ozone recovery unit monitors that the pipeline pressure is higher than the limit value or the second ozone concentration detection sensor A2 monitors that the ozone concentration of the pipeline is higher than the limit value, the third electromagnetic valve V3 is opened, and the exhaust gas reduces the pressure of the pipeline.
Examples
The water quality of the organophosphorus wastewater for producing acephate is as follows: the organic phosphorus wastewater is treated by the treatment device and the treatment method, wherein the organic phosphorus content is 4000mg/L, the inorganic phosphorus content is 35mg/L, the COD is 13000mg/L, the salt content is 5%, the pH is 9.0.
(1) The pressure in the high-pressure part section of the control device is 3Mpa, the residence reaction time of the mixture of the organic phosphorus wastewater and the ozone in the ozone main reactor R is 2.5h, the pressure in the low-pressure part section of the control device is 0.1Mpa, the mixing proportion is regulated to 50% by all mixing valves, and the ozone adding amount is controlled to 20000mg/L.
(2) The organic phosphorus wastewater is led into a first mixing valve V4 through a high-pressure pump P1, flows through a pressure-resistant circulating pump P2 and is led into an ejector E5; the oxygen enters the ozone generator E1 through the third mixing valve V6 to react to generate ozone, and the ozone is pressurized by the ozone compressor E2 and then is converged to the ejector E5 through the second mixing valve V5.
(3) The organic phosphorus wastewater and ozone are fully mixed at the ejector E5, then enter an ozone main reactor R for ozone oxidation reaction, meanwhile, 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, ozone and oxygen which are not fully reacted at 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 organic phosphorus wastewater, and the mixed wastewater enters the ozone main reactor R for continuous ozone oxidation reaction; the solubility of ozone in the ozone main reactor R can reach more than 500mg/L, and the mixture of the organic phosphorus wastewater and the ozone is fully reacted under the catalysis of the catalyst filler layer C.
(4) When the reacted wastewater liquid level reaches the position of the liquid level sensor L, the first electromagnetic valve V1 is opened by 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 the pressure sensor B1 arranged at the upper part of the liquid level sensor L of the ozone main reactor R monitors that the internal pressure of the ozone main reactor R is higher than a limit value or the ozone concentration detection sensor A1 monitors that the ozone concentration of a gas space is higher than the limit value, the electromagnetic valve V2 is opened, ozone and oxygen which are not fully reacted at the upper part of the ozone main reactor R are discharged to the ozone tail gas destructor E4 and the ozone tail gas destructor E3 through the pressure reducing valve V7, oxygen gas at the outlet of the ozone tail gas destructor E3 is collected into the ozone generator E1 through the mixing valve V6 after being dried through the drying adsorption tower T, and the recovered oxygen gas and fresh oxygen gas are mixed into the ozone generator E1 to prepare ozone. When the pressure sensor B2 on the pipeline of the ozone recovery unit monitors that the pipeline pressure is higher than the limit value or the ozone concentration detection sensor A2 on the pipeline monitors that the ozone concentration of the pipeline is higher than the limit value, the electromagnetic valve V3 on the third valve is opened, and the exhaust gas reduces the pressure of the pipeline.
The water quality of the treated organophosphorus wastewater for producing acephate is as follows: the organic phosphorus content is 5mg/L, the inorganic phosphorus content is 4030mg/L, the COD is 5000mg/L, the salt content is 5%, and the pH is 7.0. After treatment, the organic phosphorus in the wastewater is effectively removed, and simultaneously, the COD index is greatly reduced.
The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings and specific examples, but the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solutions of the present invention within the scope of the technical concept of the present invention, and all the simple modifications belong to the protection scope of the present invention.
Claims (10)
1. An organic phosphorus wastewater treatment device for producing acephate, which is characterized in that: comprises a wastewater reaction unit, an ozone preparation unit and an ozone recovery unit;
the waste water reaction unit comprises a high-pressure pump (P1), a pressure-resistant circulating pump (P2), an ejector (E5) and an ozone main reactor (R) which are sequentially connected through a pipeline, wherein the high-pressure pump (P1) is provided with an organophosphorus waste water input port, the ejector (E5) is connected with the lower inlet of the ozone main reactor (R) through the pipeline, the middle upper part of the ozone main reactor (R) is provided with a catalyst packing layer (C), and the upper part of the catalyst packing layer (C) is provided with a water outlet pipeline;
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, wherein 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;
the ozone recovery unit comprises 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), wherein the pressure reducing valve (V7) is connected with the top outlet of an ozone main reactor (R) of the wastewater reaction unit through a pipeline, and the drying adsorption tower (T) is connected with a third mixing valve (V6) of the ozone preparation unit through a pipeline.
2. The device for treating organophosphorus wastewater for producing acephate according to claim 1, wherein the device comprises: the waste water reaction unit also comprises a first mixing valve (V4), wherein the first mixing valve (V4) is arranged between the high-pressure pump (P1) and the pressure-resistant circulating pump (P2), and an inlet of the first mixing valve (V4) is connected with a middle outlet of the ozone main reactor (R) through a pipeline.
3. The device for treating organophosphorus wastewater for producing acephate according to claim 1 or 2, wherein: the upper portion of catalyst packing layer (C) in ozone main reactor (R) be provided with level sensor (L), the outlet pipe line of ozone main reactor (R) on be provided with solenoid valve (V1), solenoid valve (V1) open and close through level sensor (L) control.
4. A treatment device for 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, a first pressure sensor (B1) and a first ozone concentration detection sensor (A1) are arranged on the upper portion of the ozone main reactor (R), 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 on the upper part of the liquid level sensor (L) of the ozone main reactor (R) through a pipeline.
6. An apparatus for treating organophosphorus wastewater for producing acephate according to claim 1 or 5, wherein: the outlet of the 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 a pipeline of the ozone recovery unit, and the opening and closing of the third electromagnetic valve (V3) are controlled through the second pressure sensor (B2) and the second ozone concentration detection sensor (A2).
7. The method for treating the organophosphorus wastewater for producing acephate is characterized by comprising the following steps of:
step one, the organophosphorus 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 mixing valve III (V6) to react to generate ozone, and the ozone is converged to an ejector (E5) through a mixing valve II (V5) after the pressure of the ozone is increased through an ozone compressor (E2);
step three, after mixing the organophosphorus wastewater and ozone, introducing the mixed organophosphorus wastewater into an ozone main reactor (R) from the inlet at the lower part of the ozone main reactor (R) to perform ozone oxidation reaction, and discharging the reacted wastewater 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 jet device (E5) again through a first mixing valve (V4) and a pressure-resistant circulating pump (P2), ozone and oxygen which are not fully reacted at the upper part of the ozone main reactor (R) enter the jet device (E5) again through a second mixing valve (V5) to be mixed with the organophosphorus wastewater, and the mixed wastewater enters the ozone main reactor (R) to continuously carry out ozone oxidation reaction;
and fifthly, fully reacting the mixture of the organophosphorus wastewater and the ozone through the catalyst filler layer C, and when the liquid level of the reacted wastewater reaches the position of the liquid level sensor (L), opening the first electromagnetic valve (V1) through a feedback signal of 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 an ozone concentration detection sensor (A1) monitors that the ozone concentration of a gas space is higher than the limit value, a second electromagnetic valve (V2) is opened, ozone and oxygen which are not fully 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), residual ozone in the tail gas is destroyed by the second ozone tail gas destructor (E4) and the first ozone tail gas destructor (E3) so as to be converted into oxygen gas, and the oxygen gas at an outlet of the first ozone tail gas destructor (E3) is collected into an ozone generator (E1) through a third mixing valve (V6) after drying treatment through a drying adsorption tower T.
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 pipeline pressure 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 reduces the pressure of the pipeline.
10. The method for treating organophosphorus wastewater for producing acephate according to claim 8 or 9, wherein the method comprises the following steps: the time of the ozone oxidation reaction of the mixture of the organophosphorus wastewater and the ozone 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 3.5MPa; 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 0.1MPa.
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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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