CN221117061U - MVR coupling multi-effect rectification imidacloprid wastewater recycling device - Google Patents
MVR coupling multi-effect rectification imidacloprid wastewater recycling device Download PDFInfo
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- CN221117061U CN221117061U CN202322641993.8U CN202322641993U CN221117061U CN 221117061 U CN221117061 U CN 221117061U CN 202322641993 U CN202322641993 U CN 202322641993U CN 221117061 U CN221117061 U CN 221117061U
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- 238000004064 recycling Methods 0.000 title claims abstract description 37
- 239000002351 wastewater Substances 0.000 title claims abstract description 36
- 239000005906 Imidacloprid Substances 0.000 title claims abstract description 21
- YWTYJOPNNQFBPC-UHFFFAOYSA-N imidacloprid Chemical compound [O-][N+](=O)\N=C1/NCCN1CC1=CC=C(Cl)N=C1 YWTYJOPNNQFBPC-UHFFFAOYSA-N 0.000 title claims abstract description 21
- 229940056881 imidacloprid Drugs 0.000 title claims abstract description 21
- 230000008878 coupling Effects 0.000 title claims abstract description 11
- 238000010168 coupling process Methods 0.000 title claims abstract description 11
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 130
- 239000011550 stock solution Substances 0.000 claims abstract description 76
- 239000012153 distilled water Substances 0.000 claims abstract description 66
- 239000007788 liquid Substances 0.000 claims abstract description 58
- 238000011084 recovery Methods 0.000 claims abstract description 49
- 239000011552 falling film Substances 0.000 claims abstract description 47
- 238000004519 manufacturing process Methods 0.000 claims abstract description 33
- 238000000605 extraction Methods 0.000 claims abstract description 30
- 239000000463 material Substances 0.000 claims abstract description 29
- WRYCSMQKUKOKBP-UHFFFAOYSA-N Imidazolidine Chemical compound C1CNCN1 WRYCSMQKUKOKBP-UHFFFAOYSA-N 0.000 claims description 27
- 238000004821 distillation Methods 0.000 claims description 16
- 239000000243 solution Substances 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 8
- 239000002912 waste gas Substances 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 20
- 238000013461 design Methods 0.000 abstract description 12
- 239000000575 pesticide Substances 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 238000012546 transfer Methods 0.000 abstract description 6
- 229910052799 carbon Inorganic materials 0.000 abstract description 3
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-dimethylformamide Substances CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 23
- 238000005406 washing Methods 0.000 description 13
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 239000002994 raw material Substances 0.000 description 9
- 239000012141 concentrate Substances 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical compound CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 description 5
- 238000005086 pumping Methods 0.000 description 5
- 239000012452 mother liquor Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000003905 agrochemical Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012527 feed solution Substances 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses an MVR coupling multi-effect rectification imidacloprid wastewater recycling device which comprises a light component removal tower, a heavy component removal tower, a rectification tower, an MVR compressor, an MVR falling film reboiler, an MVR distilled water tank, a stock solution tank, a secondary stock solution heater, a stock solution pump, a light component removal condenser, a light component removal tank, a light component removal reboiler, a light component removal circulating pump, a light component removal material liquid pump and a light component removal extraction pump. The device combines the three-dimensional space-variable turbulence design method to optimally design the energy transfer equipment or the device of the multi-effect rectification system, so that the heat exchange end difference of the energy transfer equipment can be reduced, the power consumption of the energy transfer system is reduced, the energy consumption of the multi-effect rectification system is further reduced, and the low-carbon operation of the multi-effect rectification pesticide production wastewater recycling recovery system is realized.
Description
Technical Field
The utility model relates to the technical field of pesticide production wastewater recycling equipment, in particular to an MVR coupling multi-effect rectification imidacloprid wastewater recycling device.
Background
The agricultural chemical industry pollution mainly comes from the wastewater discharged in the production process, the national agricultural chemical industry discharges about 2.5 hundred million tons of wastewater each year in 2020, and the agricultural chemical industry mainly relates to the drainage, product washing water, equipment, workshop floor cleaning water and the like in the production process. Pesticide production wastewater has long been a major concern in society due to high toxicity, high concentration and difficult treatment. The technology for treating the wastewater in pesticide production can be divided into a physical and chemical method, a biochemical method and an incineration method according to the different application principles. Extraction and rectification are the most widely-used physical and chemical methods for treating the pesticide production wastewater, and because the extraction needs to use a solvent, and the solvent is recovered by combining a rectification mode, the extraction and rectification are effective modes for avoiding secondary pollution of the solvent, and the recycling of the pesticide production wastewater is convenient to realize. However, the rectification method has high energy consumption and high treatment cost. The existing multi-effect distillation equipment has the disadvantages of complex structure, long process flow, low resource utilization rate and high equipment and labor cost.
Disclosure of utility model
The utility model aims to overcome the defects of the prior art and provides an MVR coupling multi-effect rectification imidacloprid wastewater recycling device.
The utility model is realized by the following technical scheme: the MVR coupling multi-effect rectification imidacloprid wastewater recycling device comprises a stock solution tank, a secondary stock solution heater, a stock solution pump, a light-removal condenser, a light-removal tank, a light-removal reboiler, a light-removal circulating pump, a light-removal material liquid pump and a light-removal extraction pump; the primary liquid tank and the secondary primary liquid heater are arranged in front of the light component removal tower, and heat sources of the secondary primary liquid heater are respectively from recovered MVR distilled water and condensed water sensible heat of the light component removal tower and the rectifying tower; the secondary stock solution heater comprises a distilled water stock solution heater and a condensed water stock solution heater connected with the distilled water stock solution heater; the inlet of the stock solution tank is connected with stock solution from a production workshop through a connecting pipeline, the inlet of the stock solution pump is connected with the stock solution tank, and the outlet of the stock solution pump is connected with the distilled water stock solution heater; the top of the light component removing tower is respectively connected with the light component removing condenser and the light component removing tank, the bottom of the light component removing tower is connected with the bottom tube side of the light component removing reboiler through the light component removing circulating pump, and the upper tube side of the light component removing reboiler is connected with the lower part of the light component removing tower; the light component removing condenser and the light component removing tank are also connected with a light component removing vacuum pump for extracting non-condensable gas in the light component removing tower; the bottom of the light component removing tank is connected with a factory recovery system through the light component removing extraction pump; the bottom of the light component removing tower is connected with the heavy component removing tower through the light component removing liquid pump; the heat source of the light-removal reboiler is from heat steam supplied in a factory, the light-removal reboiler is connected with the condensate stock solution heater through a second condensate water recovery interface, the heating steam passes through a shell pass, latent heat is released, the heat source is connected with the condensate stock solution heater through the second condensate water recovery interface, and sensible heat is further released in the condensate stock solution heater and then recycled. Condensing the light component distilled from the top of the light component removing tower in a light component removing condenser, wherein one part of the light component is refluxed to the light component removing tower, and the other part of the light component is recycled after entering a light component removing tank; the bottom of the light component removal tower is provided with a light component removal reboiler, a heat source is from heat steam in a factory, the heat steam is sent to a shell side, latent heat is released and then is sent to a condensate stock solution heater through a second condensate recovery interface, and sensible heat is further released and then returns to a condensate collection system in the factory; a discharge pump (light material liquid removing pump) is arranged at the bottom of the light material removing tower to extract hot water containing DMF and imidazolidine to the heavy material removing tower.
The device also comprises a falling film circulating pump, a weight-removing material liquid pump, a distilled water reflux pump, a distilled water recovery pump and a first condensate water recovery interface; the top of the heavy removal tower is connected with the MVR compressor, and the MVR compressor is connected with the upper shell side of the MVR falling film reboiler; the bottom tube pass of the MVR falling film reboiler is connected with the lower part of the weight-removing tower, and the top of the tube pass of the MVR falling film reboiler is connected with the bottom of the weight-removing tower through the falling film circulating pump; the bottom of the MVR falling film reboiler shell pass is connected with the MVR distilled water tank, the outlet of the MVR distilled water tank is connected with the distilled water stock solution heater sequentially through the distilled water recovery pump and the first condensed water recovery interface, and the outlet of the MVR distilled water tank is also connected with the upper part of the de-weight tower through the distilled water reflux pump; the bottom of the heavy-removal tower is connected with the rectifying tower through the heavy-removal feed liquid pump. The vapor at the top of the heavy-duty removal tower firstly enters an MVR compressor, after enthalpy increase and temperature rise, enters the shell side of an MVR falling film reboiler at the bottom of the tower, releases latent heat and then enters an MVR distilled water tank; a falling film circulating pump is arranged at the bottom of the de-weighting tower, materials are pumped into an MVR falling film reboiler, and after falling film heating in a heater pipe, the materials flow back to the de-weighting tower; the MVR distilled water tank collects condensed water of the MVR falling film reboiler, one part of the condensed water flows back to the top of the heavy-duty removal tower, the other part of the condensed water is pumped to the distilled water stock solution heater, and the condensed water is recycled to the production water washing post after further releasing sensible heat; the bottom of the de-weighting tower is also provided with a de-weighting material liquid pump, and the mother liquor rich in imidazolidine and DMF is pumped to the rectifying tower.
The device also comprises a rectification condenser, a concentration separation tank, a rectification reboiler, a DMF concentrated solution extraction pump, an imidazolidine concentrated solution extraction pump, a forced circulation pump and a distillation vacuum pump; the top outlet of the rectifying tower is connected with the rectifying condenser, the concentration separating tank is connected with the upper inlet of the rectifying tower, and one outlet of the rectifying condenser is connected on a connecting pipeline between the concentration separating tank and the rectifying tower through a connecting pipe; the concentration separation tank is connected with the rectification condenser in parallel on the distillation vacuum pump, and is connected with a workshop waste gas treatment system through the distillation vacuum pump; the bottom of the concentration separation tank is connected with a factory recovery system through the DMF concentrated solution extraction pump rich in DMF; the bottom of the rectifying tower is connected with the bottom tube side of the rectifying reboiler through the forced circulation pump, the top of the tube side of the rectifying reboiler is connected with the lower part of the rectifying tower, the lower shell side of the rectifying reboiler is connected with the condensate water stock solution heater through a second condensate water recovery interface, and the heat source of the rectifying reboiler is from plant heating steam and enters the shell side of the rectifying reboiler; and the bottom of the rectifying tower is pumped back to a production line for application through the imidazolidine concentrated solution extraction pump. The condensate rich in DMF condensed from the rectifying condenser at the top of the rectifying tower is partially refluxed to the rectifying tower, and the other part is recycled after entering the concentrating and separating tank; a rectification reboiler is arranged at the bottom of the rectification tower, a heat source is from the heat supply steam of the factory, the second condensed water recovery interface is sent to a condensed water stock solution heater, and sensible heat is released and then returned to a condensed water collection system of the factory; the bottom of the rectifying tower is provided with a discharge pump (an imidazolidine concentrated solution extraction pump) to extract the concentrated solution rich in imidazolidine, and the concentrated solution is pumped to a recycling production line for reuse.
The MVR falling film reboiler adopts a twisted oval tube as a heat exchange tube bundle of the heater, and a guide cylinder for wrapping the heat exchange tube bundle is arranged in a cylinder body of the MVR falling film reboiler.
The light-removal reboiler and the rectification reboiler are heat exchange tube bundles which are arranged in parallel by adopting twisted elliptical tubes; the distilled water stock solution heater and the condensed water stock solution heater adopt a twisted elliptic tube shell-and-tube heat exchanger or a plate heat exchanger.
The light component removing tower and the heavy component removing tower are both in plate type tower structures, and the rectifying tower is in plate type tower structures or packed tower structures.
The heat exchange tube bundles of the shell-and-tube heater and the reboiler are bundled by a plurality of twisted elliptic tubes with high specific surface and form convex point contact among the tube bundles to form a mutual supporting structure, so that an axial multichannel circulation channel is formed, and a baffle plate or an intermediate supporting tube plate is not required to be arranged; the cross section of the twisted elliptical tube is nearly elliptical, and is twisted to form a spiral structure through secondary processing. The three-dimensional space-changing turbulence design of axial multiple channels is formed between the heat exchange tube bundles, so that the heat exchange end difference can be reduced, the energy loss can be reduced, and the heat exchange efficiency can be improved.
Compared with the prior art, the utility model has the advantages that: the device utilizes the latent heat of steam extracted from the recovery weight-removing tower as a heat source of the weight-removing reboiler, and the heat consumption of the weight-removing tower accounts for more than 80% of that of the whole multi-effect rectifying system, and the MVR device is used for enthalpy-increasing and temperature-increasing the steam extracted from the weight-removing tower and reboiling and heating the tower bottom, so that the energy consumption of the weight-removing tower can be greatly reduced, the distilled water is prevented from being cooled and recovered by adopting the tower top condenser, the energy consumption and the water consumption of a cooling system are reduced, and the energy and water conservation of the pesticide production wastewater recycling process are realized. The energy transfer equipment or device of the multi-effect rectification system is optimally designed by combining the three-dimensional space-variable turbulence design method, so that the heat exchange end difference of the energy transfer equipment can be reduced, the power consumption of the energy transfer system is reduced, the energy consumption of the multi-effect rectification system is further reduced, and the low-carbon operation of the multi-effect rectification pesticide production wastewater recycling system is realized. The reboiler operation reliability and heat exchange performance of the mutual supporting structure without baffles are obviously improved.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present utility model;
FIG. 2 is a schematic view of a partial structure of a heat exchanger tube bundle according to an embodiment of the present utility model using twisted oval tubes;
Fig. 3 is a cross-sectional view of an embodiment of the present utility model taken along a cross-sectional direction of a heat exchanger tube bundle employing a twisted oval tube.
The meaning of the reference numerals in the figures: 1. a stock solution tank; 2. a distilled water stock solution heater; 3. a condensate water stock solution heater; 4. a light component removing tower; 5. a light-off condenser; 6. a light-weight removing tank; 7. a light removal reboiler; 8. a weight removing tower; 9. an MVR compressor; 10. MVR falling film reboiler; 11. MVR distilled water tank; 12. a rectifying tower; 13. a rectification condenser; 14. concentrating a separating tank; 15. rectifying a reboiler; 161. a raw liquid pump; 162. a light-off circulation pump; 163. a light material removing liquid pump; 164. a light extraction pump; 165. a falling film circulating pump; 166. a weight-removing material liquid pump; 167. a distilled water reflux pump; 168. a distilled water recovery pump; 169. an imidazolidine concentrate extraction pump; 1610. DMF concentrate extraction pump; 1611. a forced circulation pump; 171. a light vacuum pump; 172. a distillation vacuum pump; 181. a first condensate recovery interface; 182. a second condensate recovery interface; A. a raw material liquid; B. non-condensable gas; C. heating steam in a factory; D. a factory recovery system; E. a cooling system; F. producing a water washing post; G. and a factory condensate collection system.
Detailed Description
The present utility model will be described in further detail with reference to the drawings and detailed description.
Examples
Referring to fig. 1, the method for recycling the MVR-coupled multi-effect rectification imidacloprid wastewater comprises a light component removal tower 4, a heavy component removal tower 8, a rectification tower 12, an MVR compressor 9, an MVR falling film reboiler 10 and an MVR distilled water tank 11, and the recycling method comprises the following steps:
Step one: the pesticide wastewater raw material liquid from a production workshop enters a light component removal tower 4 after being heated, and after being decompressed and separated in the light component removal tower 4, light component substances dichloroethane and methanol obtained from the top of the light component removal tower 4 are pumped to a factory recovery system D; the non-condensable gas B in the light component removal tower 4 is pumped and discharged to a workshop waste gas treatment system through a vacuum pump;
Step two: the material liquid subjected to light removal by the light removal tower 4 is pumped into the heavy removal tower 8 to be heated for flash separation, and vapor enters the MVR compressor 9 to be compressed, enthalpy-increased and temperature-raised, enters the MVR falling film reboiler 10 to release condensation latent heat and then is collected into the MVR distilled water tank 11; the material liquid and the circulating material liquid which are subjected to flash evaporation in the de-weight tower 8 are pumped to the tube side of an MVR falling film reboiler 10 through a falling film circulating pump 165, and the material liquid is refluxed to the de-weight tower after absorbing the latent heat released by the shell side steam; distilled water collected by the distilled water tank is pumped into the distilled water stock solution heater 2 to further release part of sensible heat, and the distilled water is cooled and returned to a washing workshop for recycling;
Step three: and (3) extracting part of feed liquid rich in imidazolidine and DMF from the bottom of the de-weight tower 8, pumping the feed liquid into a rectifying tower 12 after distillation, carrying out reduced pressure distillation, distilling DMF after rectification, pumping a small part of water vapor into a production line of a factory recovery system D for reuse, and cooling and recovering the remaining mother liquid rich in imidazolidine for reuse in the production line.
In the recovery method, the aim is to dissolve the imidazolidine into hot water by utilizing the difference of solubility of the imidazolidine dissolved in the dichloroethane solution of the imidacloprid, and the impurities such as DMF, dichloroethane, methanol and the like are simultaneously contained in the hot water after the imidazolidine is dissolved, and the DMF and the imidazolidine are recovered by adopting a multistage rectification process. Removing light components such as dichloroethane and methanol at the top of the light component removal tower 4; the hot water containing DMF and imidazolidine is extracted from the bottom of the light component removal tower 4, then the heavy component removal tower 8 is carried out, the MVR distillation mode is adopted in the heavy component removal tower 8, the vapor extracted from the tower top is compressed and enthalpy-increased through the MVR compressor 9 and then returns to the MVR falling film reboiler 10 at the tower bottom, heat is provided for releasing latent heat and reboiling at the tower bottom, and distilled water is recycled after the latent heat is further released by the raw material liquid heater; and (3) extracting mother liquor containing the imidazolidine and the DMF from the bottom of the de-weight tower 8, rectifying, steaming the DMF, and returning the rest mother liquor to the production line for application by cooling and recycling the imidazolidine.
The device comprises a stock solution tank 1, a secondary stock solution heater, a stock solution pump 161, a light removal condenser 5, a light removal tank 6, a light removal reboiler 7, a light removal circulating pump 162, a light removal feed solution pump 163 and a light removal extraction pump 164; a stock solution tank 1 and a secondary stock solution heater are arranged in front of the light component removal tower 4, and heat sources of the secondary stock solution heater are respectively from recovered MVR distilled water and condensed water sensible heat of the light component removal tower 4 and the rectifying tower 12; the secondary stock solution heater comprises a distilled water stock solution heater 2 and a condensed water stock solution heater 3 connected with the distilled water stock solution heater; the inlet of the stock solution tank 1 is connected with the stock solution A from a production workshop through a connecting pipeline, the inlet of the stock solution pump 161 is connected with the stock solution tank 1, and the outlet of the stock solution pump 161 is connected with the distilled water stock solution heater 2; the top of the light component removing tower 4 is respectively connected with the light component removing condenser 5 and the light component removing tank 6, the bottom of the light component removing tower 4 is connected with the bottom tube side of the light component removing reboiler 7 through the light component removing circulating pump 162, and the upper tube side of the light component removing reboiler 7 is connected with the lower part of the light component removing tower 4; the light-off condenser 5 and the light-off tank 6 are also connected with a light-off vacuum pump 171 for pumping out the non-condensable gas B in the light-off tower 4; the bottom of the light-off tank 6 is connected with a factory recovery system D through a light-off extraction pump 164; the bottom of the light component removing tower 4 is connected with a heavy component removing tower 8 through a light component removing liquid pump 163; the heat source of the light-removal reboiler 7 is from the factory heating steam C, and the light-removal reboiler 7 is connected with the condensate stock solution heater 3 through a second condensate recovery interface 182; the heating steam goes through the shell pass, releases latent heat, is connected with the condensate stock solution heater 3 through the second condensate recovery interface 182, and further releases sensible heat in the condensate stock solution heater 3 for recycling. Condensing the light component distilled from the top of the light component removing tower 4 in a light component removing condenser 5, wherein one part of the light component is refluxed to the light component removing tower 4, and the other part of the light component is recycled after entering a light component removing tank 6; the bottom of the light component removal tower 4 is provided with a light component removal reboiler 7, a heat source is from the heat supply steam C in the factory, the heat steam goes away from the shell side, latent heat is released and then is sent to the condensate stock solution heater 3 through the second condensate recovery interface 182, and sensible heat is further released and then returns to the condensate collection system G in the factory; the bottom of the light component removal tower 4 is provided with a discharge pump (light component removal feed liquid pump 163) for extracting hot water containing DMF and imidazolidine to the heavy component removal tower 8. In this embodiment, the light component removal vacuum pump 171 is provided to ensure the vacuum operation of the system while withdrawing the non-condensable gas from the light component removal column 4.
The device also comprises a falling film circulating pump 165, a weight-removing material liquid pump 166, a distilled water reflux pump 167, a distilled water recovery pump 168 and a first condensate recovery interface 181; the top of the heavy-removal tower 8 is connected with an MVR compressor 9, and the MVR compressor 9 is connected with the upper shell side of an MVR falling film reboiler 10; the bottom tube pass of the MVR falling film reboiler 10 is connected with the lower part of the heavy-duty removal tower 8, and the top of the tube pass of the MVR falling film reboiler 10 is connected with the bottom of the heavy-duty removal tower 8 through a falling film circulating pump 165; the bottom of the shell side of the MVR falling film reboiler 10 is connected with an MVR distilled water tank 11, the outlet of the MVR distilled water tank 11 is connected with a distilled water stock solution heater 2 through a distilled water recovery pump 168 and a first condensed water recovery interface 181 in sequence, and the outlet of the MVR distilled water tank 11 is also connected with the upper part of a weight removing tower 8 through a distilled water reflux pump 167; the bottom of the weight-removing tower 8 is connected with the rectifying tower 12 through a weight-removing feed liquid pump 166. The vapor at the top of the heavy-removal tower 8 firstly enters an MVR compressor 9, after enthalpy increase and temperature rise, enters the shell side of an MVR falling film reboiler 10 at the bottom of the tower, releases latent heat and then enters an MVR distilled water tank 11; a falling film circulating pump 165 is arranged at the bottom of the weight removing tower 8, materials are pumped into an MVR falling film reboiler 10, and after falling film heating in a heater pipe, the materials flow back to the weight removing tower 8; the MVR distilled water tank 11 collects condensed water of the MVR falling film reboiler 10, one part of the condensed water flows back to the top of the heavy-duty removal tower 8, the other part of the condensed water is pumped to the distilled water stock solution heater 2, and the condensed water is recycled in the production water washing station F after further releasing sensible heat; the bottom of the de-weight tower 8 is also provided with a de-weight material liquid pump 166 for pumping the mother liquor rich in imidazolidine and DMF to the rectifying tower 12.
The device also comprises a rectification condenser 13, a concentration separation tank 14, a rectification reboiler 15, a DMF concentrate extraction pump 1610, an imidazolidine concentrate extraction pump 169, a forced circulation pump 1611 and a distillation vacuum pump 172; the top outlet of the rectifying tower 12 is connected with a rectifying condenser 13, a concentrating and separating tank 14 is connected with the upper inlet of the rectifying tower 12, and an outlet of the rectifying condenser 13 is connected on a connecting pipeline between the concentrating and separating tank 14 and the rectifying tower 12 through a connecting pipe; the concentrating and separating tank 14 is connected with the rectifying condenser 13 in parallel on a distilling vacuum pump 172, and is connected with a workshop waste gas treatment system through the distilling vacuum pump 172; the bottom of the concentration separation tank 14 is connected with a factory recovery system D through a DMF concentrate extraction pump 1610; the bottom of the rectifying tower 12 is connected with the bottom tube side of the rectifying reboiler 15 through a forced circulation pump 1611, the top of the tube side of the rectifying reboiler 15 is connected with the lower part of the rectifying tower 12, the lower shell side of the rectifying reboiler 15 is connected with the condensate stock solution heater 3 through a second condensate water recovery interface 182, and the heat source of the rectifying reboiler 15 is from the factory heating steam C and enters the shell side of the rectifying reboiler 15; the bottom of the rectifying tower 12 is sent back to the production line for application through an imidazolidine concentrated solution extraction pump 169. DMF vapor distilled from a rectifying condenser 13 at the top of a rectifying tower 12 is partially refluxed to the rectifying tower 12, and the other part is recycled after entering a concentrating and separating tank 14; the bottom of the rectifying tower 12 is provided with a rectifying reboiler 15, the heat source is from the heat supply steam of the factory, the second condensate water recovery interface 182 is sent to the condensate water stock solution heater 3, and sensible heat is released and then returned to the condensate water collecting system G of the factory; the bottom of the rectifying tower 12 is provided with a discharge pump (an imidazolidine concentrated solution extraction pump 169) for extracting the concentrated solution rich in imidazolidine and pumping the concentrated solution to a recycling production line for reuse. In this embodiment, the distillation vacuum pump 172 is provided to ensure the vacuum operation of the system while withdrawing the non-condensable gas from the rectifying column 12.
In this embodiment, the raw material liquid a (wastewater from the washing process of imidacloprid production in this example) from the production shop passes through the raw material liquid tank 1, then is sent to the distilled water raw material liquid heater 2 by the raw material liquid pump 161, and after being heated, is continuously sent to the condensed water raw material liquid heater 3 for secondary heating, and then is sent to the light component removal tower 4. The heated raw material liquid A enters the light component removing tower 4, then enters a light component removing reboiler 7 together with the material liquid in the light component removing tower 4 under the action of a light component removing circulating pump 162, and returns to the light component removing tower 4 after being heated, at the moment, the high-temperature material liquid enters the light component removing tower 4 and then is decompressed and separated, light components such as dichloroethane and methanol are evaporated, and meanwhile, part of water vapor is contained, and enters a tower top light component removing condenser 5 and a light component removing tank 6 for separation, and part of condensate flows back to the tower top of the light component removing tower 4; the non-condensable gas of the light component removing system is pumped and discharged to a workshop waste gas treatment system through a light component removing vacuum pump 171, the bottom of a light component removing tank 6 is connected with a light component removing extraction pump 164 of the light component removing tower 4, and the extracted light component is pumped to a factory recovery system D.
A light-removal feed liquid pump 163 at the bottom of the light-removal tower 4 pumps the light-removal feed liquid to a heavy-removal tower 8, part of water is evaporated after the feed liquid enters the heavy-removal tower 8, the rest enters a stripping section, the feed liquid is pumped to the top of an MVR falling film reboiler 10 through a falling film circulating pump 165, and the feed liquid returns to the lower part of the heavy-removal tower 8 after being heated through a pipe side falling film; the heated feed liquid enters a de-weight tower 8 and is subjected to flash evaporation separation, wherein water vapor enters an MVR compressor 9 from the top of the tower, is compressed, enthalpy-increased and temperature-increased, enters the shell side of an MVR falling film reboiler 10, is condensed after latent heat is released, distilled water enters an MVR distilled water tank 11, a part of the distilled water is pumped to a distilled water stock solution heater 2 through a distilled water recovery pump 168, and is further cooled after partial sensible heat is released, and then returns to a water washing workshop for recycling; the other part is pumped back to the top of the weight removal column 8 by a distilled water reflux pump 167.
A heavy material removing liquid pump 166 at the bottom of the light and heavy tower pumps distilled material liquid to the rectifying tower 12, the material liquid enters the rectifying tower 12 and then enters a forced circulation pump 1611 together with circulating material liquid, the material liquid is pumped into a rectifying reboiler 15 through the forced circulation pump 1611 and returns to the rectifying tower 12 after being heated, the material liquid with high temperature enters the rectifying tower 12 and then is decompressed and rectified, DMF and part of water vapor enter a rectifying condenser 13 and a concentrating separation tank 14, and part of condensate liquid flows back to the top of the rectifying tower 12; the non-condensable gas of the light removal system is pumped and discharged to a workshop waste gas treatment system through a light removal vacuum pump 171, the bottom of a concentration separation tank 14 is connected with a DMF concentrate extraction pump 1610, and the extracted DMF concentrate is pumped to a factory recovery system D; an imidazolidine concentrated solution extraction pump 169 is arranged at the bottom of the rectifying tower 12, and the DMF-removed feed liquid is pumped to a washing workshop for recycling.
The method for recycling wastewater in the washing process of MVR coupling multi-effect rectification imidacloprid production aims to develop a method technology for recycling wastewater in pesticide production by multi-effect rectification treatment of a coupling MVR heat pump, and combines a design method of three-dimensional turbulence heat exchange equipment, so that the waste heat in the multi-effect rectification process is utilized to the maximum extent, the energy utilization level of recycling wastewater in pesticide production by multi-effect rectification treatment is improved, and the energy cost for recycling wastewater is greatly reduced; the design method of the three-dimensional turbulence heat exchange equipment is adopted to optimally design the heat exchange equipment or the device of the multi-effect rectifying system, and the heat exchange end difference can be reduced to the greatest extent by combining the design of the self-supporting structure of the twisted elliptical tube and the parallel flow heat exchange form, so that the heat exchange efficiency of the heat exchange device is improved, and the operation reliability of the heat exchange device is improved.
Compared with a distillation system represented by multi-effect rectification or single-effect MVR heat pump distillation, the MVR coupling multi-effect rectification imidacloprid production water washing process wastewater recycling recovery method of the embodiment can reduce heat exchange temperature and pressure of the MVR heat exchange equipment, reduce MVR compression power consumption, furthest utilize waste heat resources of a rectification system and greatly improve the wastewater recycling recovery energy level due to the adoption of the heat exchange equipment of the three-dimensional turbulence design and optimization method. Taking the embodiment as an example, after the MVR coupling multi-effect rectification imidacloprid production water washing procedure wastewater recycling recovery process is adopted, the unit imidazolidine recovery energy consumption is reduced by more than 75 percent compared with the traditional single-effect distillation system; compared with the traditional three-effect rectification imidacloprid production water washing process wastewater recycling recovery process, the unit imidazolidine recovery energy consumption is reduced by 30-50%; in addition, due to the adoption of MVR technology, a water condenser is not required to be adopted, and the energy consumption and the water consumption of a cooling system are greatly reduced. Therefore, the embodiment can effectively reduce the recycling energy consumption of the wastewater in the water washing process of imidacloprid production, and realize the recycling of pesticide wastewater with low carbon.
In this embodiment, the light component removal condenser 5 and the rectification condenser 13 are both connected to the cooling system E.
The MVR falling film reboiler 10 adopts a twisted oval tube as a heat exchange tube bundle of a heater, and a guide cylinder for wrapping the heat exchange tube bundle is arranged in a cylinder of the MVR falling film reboiler 10.
The light-removal reboiler 7 and the rectification reboiler 15 are heat exchange tube bundles which are formed by arranging twisted oval tubes in parallel; the distilled water stock solution heater 2 and the condensed water stock solution heater 3 adopt a twisted elliptic tube shell-and-tube heat exchanger or a plate heat exchanger.
The light component removing tower 4 and the heavy component removing tower 8 are both in plate type tower structures, and the rectifying tower 12 is in plate type tower structures or packed tower structures.
The heat exchange tube bundles of the shell-and-tube heater and the reboiler are bundled by a plurality of twisted elliptic tubes with high specific surface and form convex point contact among the tube bundles to form a mutual supporting structure, so that an axial multichannel circulation channel is formed, and a baffle plate or an intermediate supporting tube plate is not required to be arranged; the cross section of the twisted elliptical tube is nearly elliptical, and is twisted to form a spiral structure through secondary processing. The three-dimensional space-changing turbulence design of axial multiple channels is formed between the heat exchange tube bundles, so that the heat exchange end difference can be reduced, the energy loss can be reduced, and the heat exchange efficiency can be improved. The heat exchange tube bundle adopts the twisted elliptic tubes with high specific surface, and the twisted elliptic tubes are mutually supported by convex points to form a stable structure, so that the heat exchange effect is good, and the heat recovery is facilitated. The three-dimensional variable space along turbulent flow design of the axial multiple channels is formed between the heat exchange tube bundles, and the twisted elliptic tube with the near elliptic cross section design ensures that no dead angle flows in the three-dimensional variable space, no vortex point exists, no abrasion angle exists, and no scaling and dust accumulation are formed.
With respect to the use of the heat exchange tube, referring to fig. 2 to 3, only a single twisted oval tube is shown in fig. 2, and if a plurality of twisted oval tubes are arranged in parallel, the adjacent twisted oval tubes are supported by protruding bumps.
The foregoing detailed description is directed to embodiments of the utility model which are not intended to limit the scope of the utility model, but rather to cover all modifications and variations within the scope of the utility model.
Claims (7)
1. MVR coupling multi-effect rectification imidacloprid waste water recycling device, its characterized in that: the device comprises a light component removing tower, a heavy component removing tower, a rectifying tower, an MVR compressor, an MVR falling film reboiler, an MVR distilled water tank, a stock solution tank, a secondary stock solution heater, a stock solution pump, a light component removing condenser, a light component removing tank, a light component removing reboiler, a light component removing circulating pump, a light component removing material liquid pump and a light component removing extraction pump; the primary liquid tank and the secondary primary liquid heater are arranged in front of the light component removal tower, and heat sources of the secondary primary liquid heater are respectively from recovered MVR distilled water and condensed water sensible heat of the light component removal tower and the rectifying tower; the secondary stock solution heater comprises a distilled water stock solution heater and a condensed water stock solution heater connected with the distilled water stock solution heater; the inlet of the stock solution tank is connected with stock solution from a production workshop through a connecting pipeline, the inlet of the stock solution pump is connected with the stock solution tank, and the outlet of the stock solution pump is connected with the distilled water stock solution heater; the top of the light component removing tower is respectively connected with the light component removing condenser and the light component removing tank, the bottom of the light component removing tower is connected with the bottom tube side of the light component removing reboiler through the light component removing circulating pump, and the upper tube side of the light component removing reboiler is connected with the lower part of the light component removing tower; the light component removing condenser and the light component removing tank are also connected with a light component removing vacuum pump for extracting non-condensable gas in the light component removing tower; the bottom of the light component removing tank is connected with a factory recovery system through the light component removing extraction pump; the bottom of the light component removing tower is connected with the heavy component removing tower through the light component removing liquid pump; the heat source of the light-removal reboiler is from heat steam supplied by a factory, the heat steam goes through a shell side, latent heat is released, the heat source is connected with the condensate water stock solution heater through a second condensate water recovery interface, and sensible heat is further released in the condensate water stock solution heater and then is recycled.
2. The MVR-coupled multi-effect rectification imidacloprid wastewater recycling device according to claim 1, characterized in that: the device also comprises a falling film circulating pump, a weight-removing material liquid pump, a distilled water reflux pump, a distilled water recovery pump and a first condensate water recovery interface; the top of the heavy removal tower is connected with the MVR compressor, and the MVR compressor is connected with the upper shell side of the MVR falling film reboiler; the bottom tube pass of the MVR falling film reboiler is connected with the lower part of the weight-removing tower, and the top of the tube pass of the MVR falling film reboiler is connected with the bottom of the weight-removing tower through the falling film circulating pump; the bottom of the MVR falling film reboiler shell pass is connected with the MVR distilled water tank, the outlet of the MVR distilled water tank is connected with the distilled water stock solution heater sequentially through the distilled water recovery pump and the first condensed water recovery interface, and the outlet of the MVR distilled water tank is also connected with the upper part of the de-weight tower through the distilled water reflux pump; the bottom of the heavy-removal tower is connected with the rectifying tower through the heavy-removal feed liquid pump.
3. The MVR-coupled multi-effect rectification imidacloprid wastewater recycling device according to claim 2, characterized in that: the device also comprises a rectification condenser, a concentration separation tank, a rectification reboiler, a DMF concentrated solution extraction pump, an imidazolidine concentrated solution extraction pump, a forced circulation pump and a distillation vacuum pump; the top outlet of the rectifying tower is connected with the rectifying condenser, the concentration separating tank is connected with the upper inlet of the rectifying tower, and one outlet of the rectifying condenser is connected on a connecting pipeline between the concentration separating tank and the rectifying tower through a connecting pipe; the concentration separation tank is connected with the rectification condenser in parallel on the distillation vacuum pump, and is connected with a workshop waste gas treatment system through the distillation vacuum pump; the bottom of the concentration separation tank is connected with a factory recovery system through the DMF concentrated liquid extraction pump; the bottom of the rectifying tower is connected with the bottom tube side of the rectifying reboiler through the forced circulation pump, the top of the tube side of the rectifying reboiler is connected with the lower part of the rectifying tower, the lower shell side of the rectifying reboiler is connected with the condensate water stock solution heater through a second condensate water recovery interface, and the heat source of the rectifying reboiler is from plant heating steam and enters the shell side of the rectifying reboiler; and the bottom of the rectifying tower is pumped back to a production line for application through the imidazolidine concentrated solution extraction pump.
4. The MVR-coupled multi-effect rectification imidacloprid wastewater recycling device according to claim 2, characterized in that: the MVR falling film reboiler adopts a twisted oval tube as a heat exchange tube bundle of the heater, and a guide cylinder for wrapping the heat exchange tube bundle is arranged in a cylinder body of the MVR falling film reboiler.
5. The MVR-coupled multi-effect rectification imidacloprid wastewater recycling device according to claim 3, characterized in that: the light-removal reboiler and the rectification reboiler are heat exchange tube bundles which are arranged in parallel by adopting twisted elliptical tubes; the distilled water stock solution heater and the condensed water stock solution heater adopt a twisted elliptic tube shell-and-tube heat exchanger or a plate heat exchanger.
6. The MVR-coupled multi-effect rectification imidacloprid wastewater recycling device according to claim 1, characterized in that: the light component removing tower and the heavy component removing tower are both in plate type tower structures, and the rectifying tower is in plate type tower structures or packed tower structures.
7. The MVR-coupled multi-effect rectification imidacloprid wastewater recycling device according to claim 5, characterized in that: the heat exchange tube bundles of the shell-and-tube heater and the reboiler are bundled by a plurality of twisted elliptic tubes with high specific surface and form convex point contact among the tube bundles to form a mutual supporting structure, so that an axial multichannel circulation channel is formed, and a baffle plate or an intermediate supporting tube plate is not required to be arranged; the cross section of the twisted elliptical tube is nearly elliptical, and is twisted to form a spiral structure through secondary processing.
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| CN202322641993.8U CN221117061U (en) | 2023-09-25 | 2023-09-25 | MVR coupling multi-effect rectification imidacloprid wastewater recycling device |
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| CN202322641993.8U CN221117061U (en) | 2023-09-25 | 2023-09-25 | MVR coupling multi-effect rectification imidacloprid wastewater recycling device |
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