CN210103795U - Carbendazim clean production system - Google Patents
Carbendazim clean production system Download PDFInfo
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- CN210103795U CN210103795U CN201920792744.XU CN201920792744U CN210103795U CN 210103795 U CN210103795 U CN 210103795U CN 201920792744 U CN201920792744 U CN 201920792744U CN 210103795 U CN210103795 U CN 210103795U
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Abstract
The utility model discloses a carbendazim clean production system belongs to pesticide chemical industry technical field. Comprises a lime nitrogen hydrolysis unit, an amination unit, a condensation unit, a water washing centrifugal unit and a drying unit which are connected in sequence. The lime nitrogen hydrolysis unit receives lime nitrogen and sodium carbonate, independent hydrolysis is carried out on the lime nitrogen to generate cyanamide, the cyanamide is pumped to the amination unit, the amination unit finishes amination reaction, the condensation unit finishes condensation reaction, the washing centrifugal unit carries out multi-stage washing, and the drying unit carries out drying. Through setting up lime nitrogen hydrolysis unit, mix the hydrolysis with lime nitrogen and sodium carbonate solution at the hydrolysis kettle, calcium ion and carbonate ion generation calcium carbonate turbid liquid in the mixed solution, through decalcification pressure filter press filter, get rid of most calcium ion in advance, avoid a large amount of calcium ions scale deposit in the reaction system to cause equipment pipeline to block up, prolonged production operation cycle by a wide margin, equipment process flow is simple, and the running cost is low, has huge environmental benefit.
Description
Technical Field
The utility model belongs to the technical field of the pesticide chemical industry, concretely relates to carbendazim clean production system.
Background
The carbendazim is an efficient, broad-spectrum and safe systemic fungicide, and can be used for preventing and treating leaf spot disease, black spot disease and stem rot of peanuts, gibberellic disease of wheat, black spot disease of cereals, sclerotinia rot of rape, banded sclerotial blight of rice, canker of citrus, storage diseases, fusarium wilt of melons, root rot and stem rot of flowers and plants and the like. In addition, the carbendazim has wide application prospects in the aspects of textile, printing and dyeing, papermaking, leather making, wood preservation and the like.
The main preparation process of the domestic carbendazim is a lime nitrogen method. Hydrolyzing lime nitrogen to prepare calcium cyanamide, filtering to remove residue, esterifying calcium cyanamide solution with methyl chloroformate to obtain calcium cyanamide methyl formate solution, and condensing with o-phenylenediamine to obtain carbendazim. The process mainly has the following problems that firstly, the quality and the yield of carbendazim are influenced due to the existence of calcium ions in the condensation reaction process; secondly, due to the existence of calcium ions, the pipeline of the equipment is easy to block, and the production period is short; thirdly, the generated wastewater contains a large amount of calcium chloride and ammonium chloride, the treatment difficulty is large, and the resource utilization is difficult.
In the prior art, methods for removing calcium ions comprise carbon dioxide decalcification, ion exchange resin decalcification and electrodialysis decalcification, but the methods have the problems of long process flow, complex operation and high decalcification cost.
Disclosure of Invention
In view of this, the utility model provides a clean production system of carbendazim that lime nitrogen independently hydrolysises, reduces system calcium ion, and process flow is simple.
The utility model provides a technical scheme that its technical problem adopted is:
a carbendazim clean production system comprises a lime nitrogen hydrolysis unit, an amination unit, a condensation unit, a water washing centrifugal unit and a drying unit which are connected in sequence;
the lime nitrogen hydrolysis unit receives lime nitrogen and sodium carbonate conveyed from the outside, independently hydrolyzes the lime nitrogen to generate cyanamide, and pumps the cyanamide to the amination unit; the amination unit receives cyanamide conveyed by the lime nitrogen hydrolysis unit and methyl chloroformate and liquid alkali conveyed from the outside, completes amination reaction, and conveys amination reaction liquid to the condensation unit; the condensation unit receives the amination reaction liquid conveyed by the amination unit and o-phenylenediamine, hydrochloric acid and formaldehyde conveyed from the outside, finishes condensation reaction and outputs the condensation reaction liquid to the washing centrifugal unit; the water washing centrifugal unit receives the condensation reaction liquid output by the condensation unit, carries out multi-stage water washing, and conveys wet carbendazim obtained after water washing to the drying unit; the drying unit receives the wet carbendazim conveyed by the water washing centrifugal unit and dries the wet carbendazim.
Preferably, the lime nitrogen hydrolysis unit comprises a mixing ground pool, a hydrolysis kettle, a decalcification filter press and a cyanamide intermediate storage tank which are connected in sequence;
the mixing and stirring tank is arranged on the mixing tank, receives the lime nitrogen and sodium carbonate solution, uniformly mixes the lime nitrogen and the sodium carbonate solution under the stirring action of the mixing and stirring tank, and pumps the mixed solution of the lime nitrogen and the sodium carbonate to the hydrolysis kettle; the hydrolysis kettle receives the mixed liquid of the lime nitrogen and the sodium carbonate pumped by the mixing ground pool, completes the hydrolysis of the lime nitrogen, and conveys the hydrolysate to the decalcification filter press; the decalcification filter press receives the hydrolysate conveyed by the hydrolysis kettle, performs filter pressing on the hydrolysate, separates cyanamide, and conveys the cyanamide to a cyanamide intermediate storage tank; the intermediate storage tank for cyanamide receives and temporarily stores the cyanamide delivered by the decalcification filter press and pumps the cyanamide to the amination unit.
Preferably, the lime nitrogen hydrolysis unit further comprises a filter residue pulping tank, a secondary filter press and a filtrate tank which are connected in sequence, wherein the pulping tank is connected with a filter residue outlet of the decalcification filter press; the pulping tank receives the filter residue from the decalcification filter press, pulps the filter residue, and conveys the slurry to the secondary filter press; the secondary filter press receives the slurry conveyed by the pulping tank, performs filter pressing on the slurry, conveys filtrate to the filtrate tank, and conveys filter residues to a slag discharge plant; the filtrate tank receives filtrate from a secondary filter press and pumps the filtrate to the compounding ground pool.
Preferably, the amination unit comprises an amination kettle, and a methyl chloroformate feeding buffer tank and a liquid alkali feeding buffer tank which are connected with the amination kettle, wherein the methyl chloroformate feeding buffer tank receives methyl chloroformate feeding and dropwise adds methyl chloroformate to the amination kettle, the liquid alkali feeding buffer tank receives liquid alkali feeding and dropwise adds liquid alkali to the amination kettle, the amination kettle receives cyanamide pumped by the hydrolysis unit, the methyl chloroformate dropwise added by the methyl chloroformate feeding buffer tank and the liquid alkali dropwise added by the liquid alkali feeding buffer tank, amination reaction is completed, and amination reaction liquid is output to the condensation unit.
Preferably, a weighing module is arranged on the methyl chloroformate feeding buffer tank.
Preferably, a nitrogen feeding line is arranged on the amination kettle.
Preferably, the condensation unit comprises a condensation kettle, the condensation kettle receives the amination reaction liquid conveyed by the amination unit and the hydrochloric acid, the o-phenylenediamine and the formaldehyde feed, completes condensation reaction, generates carbendazim crude liquid, and conveys the carbendazim crude liquid to the water washing centrifugal unit.
Preferably, the washing centrifugal unit comprises a washing tank, a belt vacuum filter, a carbendazim beating tank and a carbendazim centrifuge which are connected in sequence, the washing tank is filled with desalted water for washing, the belt vacuum filter receives crude carbendazim liquid conveyed by the condensation unit and desalted water pumped by the washing device, washing of the crude carbendazim liquid is completed under the condition of vacuum, and the washed carbendazim is conveyed into the carbendazim beating tank; the carbendazim pulping tank receives the carbendazim solid conveyed by the belt vacuum filter, water is added to pulp the carbendazim, and the pulped carbendazim is conveyed to the carbendazim centrifuge; and the carbendazim centrifuge receives the pulped carbendazim conveyed by the carbendazim pulping tank, performs centrifugal separation to obtain wet carbendazim, and conveys the wet carbendazim to the drying unit.
Preferably, the carbendazim clean production system further comprises a tail gas absorption unit, wherein the tail gas absorption unit comprises a draught fan, a primary alkali washing tower and a secondary alkali washing tower which are sequentially connected, and the inlet end of the draught fan is respectively connected with the lime nitrogen hydrolysis unit, the amination unit, the condensation unit, the water washing centrifugal unit and the drying unit so as to collect tail gas generated in the carbendazim production process and enable the tail gas to sequentially pass through the primary alkali washing tower and the secondary alkali washing tower for alkali washing and discharging.
Preferably, the carbendazim clean production system further comprises a water treatment unit, wherein the water treatment unit comprises a decoloring device, a desalting device and a biochemical reaction tank which are sequentially connected;
the decoloring device is used for respectively receiving wastewater generated in the production process of the lime nitrogen hydrolysis unit, the amination unit, the condensation unit, the water washing centrifugal unit and the drying unit, decoloring the wastewater and conveying the decolored wastewater to the desalting device; the desalting device receives the decolored wastewater conveyed by the decoloring device, carries out desalting treatment on the decolored wastewater, and conveys the desalted wastewater to the biochemical reaction tank; and the biochemical reaction tank receives the desalted wastewater conveyed by the desalting device, carries out biochemical treatment on the desalted wastewater, and conveys the biochemically treated wastewater to a municipal sewage pipe network.
According to the above technical scheme, the utility model provides a carbendazim clean production system, its beneficial effect is: firstly, mixing and hydrolyzing the lime nitrogen and a sodium carbonate solution in the hydrolysis kettle by arranging the lime nitrogen hydrolysis unit, generating calcium carbonate suspension by calcium ions and carbonate ions in the mixed solution, filtering to remove filter residues, and collecting filtrate, wherein the content of cyanamide in the filtrate is more than or equal to 90g/L, and the content of dicyandiamide in the filtrate is less than or equal to 6000mg/L, so that the production requirement of carbendazim can be met. Therefore, most calcium ions are removed in advance, the scale formation of a large amount of calcium ions in a reaction system is avoided, the pipeline of the equipment is prevented from being blocked, and the production operation period is greatly prolonged. Meanwhile, the equipment process flow is simple, and the operation cost is only slightly increased compared with the traditional technology. Secondly, calcium ions are extracted and removed from the reaction system, so that the discharge amount of waste water in the carbendazim production process is reduced, the content of the calcium ions in the waste water produced in the carbendazim production process is greatly reduced, the content of the calcium ions in the treated waste water is reduced to less than 1000mg/L from more than 32000mg/L in the traditional process, and great environmental benefits are obtained.
Drawings
FIG. 1 is a block diagram of a carbendazim clean production system flow.
FIG. 2 is a schematic pipeline flow diagram of a lime nitrogen hydrolysis unit.
FIG. 3 is a schematic pipeline flow diagram of the amination unit.
FIG. 4 is a schematic pipeline flow diagram of a condensation unit.
FIG. 5 is a schematic pipeline flow diagram of a water wash centrifuge unit.
FIG. 6 is a schematic pipeline flow diagram of the drying unit.
FIG. 7 is a schematic pipeline flow diagram of a tail gas absorption unit.
FIG. 8 is a schematic pipeline flow diagram of a wastewater treatment unit.
In the figure: the carbendazim cleaning production system 10, a lime nitrogen hydrolysis unit 100, a mixing ground pool 110, a lime nitrogen feeding pipe 111, a sodium carbonate feeding pipe 112, mixing stirring 113, a mixed liquid discharging pump 114, a feeding conveyor belt 115, a hydrolysis kettle 120, hydrolysis stirring 121, a decalcification filter press 130, a hydrolysis liquid filter press tank 131, homogenizing stirring 132, a filter press feeding pump 133, a cyanamide intermediate storage tank 140, a cyanamide discharging pump 141, a filter residue pulping tank 150, a water inlet pipe 151, a pulping stirring 152, a secondary filter press feeding pump 153, a secondary filter press 160, a filtrate tank 170, a filtrate discharging pump 171, a sodium carbonate preparation tank 180, a sodium carbonate feeding pipe 181, sodium carbonate homogenizing stirring 182, a sodium carbonate discharging pump 183, an amination unit 200, an amination kettle 210, a refrigeration jacket 211, amination stirring 212, a cyanamide-based discharging pump 213, a nitrogen feeding pipeline 214, a methyl chloroformate feeding buffer tank 220, a liquid alkali feeding buffer tank 230, a sodium, Methyl chloroformate storage tank 240, methyl chloroformate feed pump 241, weighing module 242, liquid caustic soda storage tank 250, liquid caustic soda feed pump 251, amino intermediate storage tank 260, condensation unit 300, condensation kettle 310, cyanamide-based feed pipe 311, o-phenylenediamine feed pipe 312, formaldehyde feed pipe 313, hydrochloric acid feed pipe 314, condensation stirring 315, carbendazim crude liquid discharge pump 316, condensation tower 320, gas phase feed pipe 321, gas phase discharge pipe 322, condensate reflux pipe 323, water washing centrifugal unit 400, water washing tank 410, water washing liquid discharge pump 411, belt vacuum filter 420, carbendazim pulping tank 430, carbendazim slurry discharge pump 431, carbendazim centrifuge 440, centrifugal water collection tank 450, centrifugal water discharge pump 451, carbendazim conveying device 460, drying unit 500, fluidized bed dryer 510, cyclone dust collector 520, bag dust collector 530, tail gas absorption unit 600, induced draft fan 610, primary alkaline washing tower 620, wet dust collection tank 460, drying unit 500, a primary alkaline washing pump 621, a secondary alkaline washing tower 630, a secondary alkaline washing pump 631, a wastewater treatment unit 700, a decoloring device 710, a desalting device 720 and a biochemical reaction tank 730.
Detailed Description
For the convenience of understanding, the technical solutions and the technical effects of the embodiments of the present invention will be further elaborated below with reference to the drawings of the present invention.
Referring to fig. 1, in an embodiment of the present invention, a carbendazim cleaning production system 10 includes a lime nitrogen hydrolysis unit 100, an amination unit 200, a condensation unit 300, a water washing centrifugal unit 400, and a drying unit 500, which are connected in sequence.
The lime nitrogen hydrolysis unit 100 receives raw materials of lime nitrogen and sodium carbonate, independently hydrolyzes the lime nitrogen to generate cyanamide, and pumps the cyanamide to the amination unit 200.
Referring to fig. 2, specifically, the lime nitrogen hydrolysis unit 100 includes a mixing ground pool 110, a hydrolysis kettle 120, a decalcification filter press 130 and a cyanamide intermediate storage tank 140, which are connected in sequence, the mixing ground pool 110 is provided with a lime nitrogen feed pipe 111, a sodium carbonate feed pipe 112, a mixing stirrer 113 and a mixed liquid discharge pump 114, one end of the lime nitrogen feed pipe 111, which is far away from the mixing ground pool 110, is connected with a feed conveyor belt 115, lime nitrogen passes through the feed conveyor belt 115, and is conveyed into the mixing ground pool 110 through the lime nitrogen feed pipe 111, meanwhile, a sodium carbonate solution enters the mixing ground pool 110 through the sodium carbonate feed pipe 112, and is uniformly mixed under the action of the mixing stirrer 113 at normal temperature, and a mixed solution of sodium carbonate and lime nitrogen is pumped into the hydrolysis kettle 120 through the mixed liquid discharge pump 114.
The hydrolysis kettle 120 is provided with a hydrolysis stirring device 121, the sodium carbonate and lime nitrogen mixed liquid pumped by the mixed liquid discharging pump 114 enters the hydrolysis kettle 120 from the upper part of the hydrolysis kettle 120, hydrolysis reaction is carried out under the stirring action of the hydrolysis stirring device 121 at the temperature of 20-30 ℃, after certain retention time, the hydrolysis reaction is finished, the hydrolysate after reaction automatically flows into the decalcification filter press 130 by gravity or is pumped into the decalcification filter press 130, and decalcification treatment is carried out on the hydrolysis reaction liquid.
A hydrolysate pressure filtration tank 131 is arranged in front of the decalcification filter press 130, a homogenizing stirring 132 and a pressure filtration feeding pump 133 are arranged on the hydrolysate pressure filtration tank 131, hydrolysate which is subjected to reaction automatically flows into the hydrolysate pressure filtration tank 131 by gravity or is pumped into the hydrolysate pressure filtration tank 131, secondary homogenization is performed under the action of the homogenizing stirring 132, and hydrolysate in the hydrolysate pressure filtration tank 131 is pumped into the decalcification filter press 130 by the pressure filtration feeding pump 133 to be subjected to pressure filtration. After filter pressing, the filtrate is conveyed to the intermediate storage tank 140 for storage and collection, a single cyanamide discharge pump 141 is arranged on the intermediate storage tank 140, and the single cyanamide discharge pump 141 is used for pumping the decalcified filtrate containing the single cyanamide of the intermediate storage tank 140 to the amination unit 200 to serve as a raw material for amination reaction. The filter residue is further treated and discharged to a slag discharge plant.
Further, lime nitrogen hydrolysis unit 100 is still including filter residue pulping tank 150, secondary filter press 160 and filtrate groove 170, be provided with inlet tube 151, making beating stirring 152 and secondary filter press charge pump 153 on the filter residue pulping tank 150, lime nitrogen hydrolysate warp decalcification filter press 130 filter pressing, the filter residue that contains high concentration calcium carbonate of production gets into in the filter residue pulping tank 150, through inlet tube 151 adds industrial water make beating water washing under the effect of making beating stirring 152 to with calcium carbonate on adnexed cyanamide and the lime nitrogen and the sodium carbonate of not complete hydrolysis and the separation of calcium carbonate turbid liquid, filter residue after the slurrying via secondary filter press charge pump 153 pump sends to secondary filter press 160 carries out the filter pressing, and the filtrating after the filter pressing carry to recycle in filtrate groove 170, the filter residue is arranged outward to arrange the row's of slag factory.
Further, a filtrate discharge pump 171 is arranged on the filtrate tank 170, the lime nitrogen hydrolysis unit 100 further includes a sodium carbonate solution preparation tank 180, a sodium carbonate feed pipe 181, a sodium carbonate homogeneous stirring 182 and a sodium carbonate discharge pump 183 are arranged on the sodium carbonate solution preparation tank 180, the filtrate discharge pump 171 pumps the secondary filter pressing filtrate stored in the filtrate tank 170 to the sodium carbonate solution preparation tank 180, a proper amount of sodium carbonate solid is added into the sodium carbonate solution preparation tank 180 through the sodium carbonate feed pipe 181, a sodium carbonate solution is prepared under the action of the sodium carbonate homogeneous stirring 182, and an outlet of the sodium carbonate discharge pump 183 is connected to the sodium carbonate feed pipe 112, so that the sodium carbonate solution is pumped to the mixing ground tank 110.
The lime nitrogen hydrolysis unit 100 realizes the independent hydrolysis of lime nitrogen and separates most of calcium ions after independent hydrolysis from the reaction system, thereby greatly reducing the content of calcium ions in the wastewater and enabling the carbendazim wastewater to have the possibility of resource recycling. And secondly, pulping and washing filter residues generated after the first filter pressing of the hydrolysate, and using the washing liquid generated by the filter pressing of the secondary filter press 160 for preparing a sodium carbonate solution, so that the part of the washing liquid returns to the reaction system again to participate in the reaction, thereby not only recycling the cyanamide attached to the calcium carbonate and the incompletely hydrolyzed lime nitrogen and sodium carbonate, improving the utilization rate of raw materials, but also reducing the yield of wastewater and obtaining good environmental benefits.
Referring to fig. 3, the amination unit 200 receives the cyanamide and the methyl chloroformate pumped by the lime nitrogen hydrolysis unit 100 and the liquid alkali, completes the amination reaction, and outputs the amination reaction liquid to the condensation unit 300.
Specifically, the amination unit 200 includes an amination kettle 210, a methyl chloroformate feeding buffer tank 220, a caustic soda liquid feeding buffer tank 230, a methyl chloroformate storage tank 240 and a caustic soda liquid storage tank 250, the methyl chloroformate feeding pump 241 is disposed on the methyl chloroformate storage tank 240, the caustic soda liquid storage tank 250 is disposed with a caustic soda liquid feeding pump 251, a discharge end of the methyl chloroformate feeding pump 241 is connected to the methyl chloroformate feeding buffer tank 220, a discharge end of the caustic soda liquid feeding pump 251 is connected to the caustic soda liquid feeding buffer tank 230, and the amination kettle 210 is connected to the methyl chloroformate feeding buffer tank 220 and the caustic soda liquid feeding buffer tank 230 to receive the methyl chloroformate and the caustic soda liquid dripped from the methyl chloroformate feeding buffer tank 220 and the caustic soda liquid feeding buffer tank 230.
The amination kettle 210 is provided with a refrigeration jacket 211, and the refrigeration jacket 211 adopts cooling water for refrigeration. The amination kettle is further provided with amination stirring 212, hydrolysate containing high-concentration cyanamide pumped by the lime nitrogen hydrolysis unit 100 enters the amination kettle 210, the kettle temperature of the amination kettle 210 is less than or equal to 30 ℃ by adjusting the flow rate of cooling water, methyl chloroformate and liquid alkali are simultaneously dripped into the amination kettle 210 through the methyl chloroformate feeding buffer tank 220 and the liquid alkali feeding buffer tank 230, amination reaction is carried out under the action of the amination stirring 212, after a certain retention time, when the pH value of amination liquid in the amination kettle 210 is 7-8, the amination reaction is finished, and heat is preserved for 0.5-2 h.
The amination unit further comprises a cyanamide intermediate storage tank 260, a cyanamide-based discharge pump 213 is arranged at the bottom of the amination kettle 210, the feed end of the cyanamide-based discharge pump 213 is connected with the amination kettle 210 and the cyanamide intermediate storage tank 260, and the discharge end of the cyanamide-based discharge pump is connected with the condensation unit 300 and the cyanamide intermediate storage tank 260. So as to temporarily store the amination reaction solution in the cyanamide-based intermediate storage tank 260 when the condensation unit 300 is operated at a low load and to supplement the shortage of the production capacity of the amination unit 200 when the condensation unit 300 is operated at a high load.
Preferably, the methyl chloroformate feed buffer 240 is further provided with a weighing module 242 for monitoring the dropping amount of methyl chloroformate.
Preferably, a nitrogen feeding line 214 is further disposed on the amination kettle 210 to introduce nitrogen into the amination kettle 210 during the amination reaction, so that the amination reaction is performed in a circulating nitrogen atmosphere, and the safety and reliability of the reaction process are ensured.
Referring to fig. 4, the condensation unit 300 receives the amination reaction solution and o-phenylenediamine, hydrochloric acid and formaldehyde outputted from the amination unit 200, completes the condensation reaction, and outputs the condensation reaction solution to the water washing centrifugal unit 400.
Specifically, the condensation unit 300 includes a condensation kettle 310, the condensation kettle 310 is provided with a cyanamide group feed pipe 311, an o-phenylenediamine feed pipe 312, a formaldehyde feed pipe 313, a hydrochloric acid feed pipe 314, and a condensation stirring 315, the cyanamide group feed pipe 311 is connected to the cyanamide group discharge pump 213, an amination reaction liquid generated by amination reaction is pumped out from the cyanamide group discharge pump 213, enters the condensation kettle 310 through the cyanamide group feed pipe 311, and is mixed with o-phenylenediamine entering the condensation kettle 310 through the o-phenylenediamine feed pipe 312, formaldehyde entering the condensation kettle 310 through the formaldehyde feed pipe 313 is mixed with hydrochloric acid entering the condensation kettle 310 through the hydrochloric acid feed pipe 314, and condensation reaction is performed under the action of the condensation stirring 315 to generate a crude carbendazim liquid. The bottom of the condensation kettle 310 is provided with a carbendazim crude liquid discharge pump 316 for completing the condensation reaction, and the generated carbendazim crude liquid is pumped to the washing centrifugal unit 400.
Further, the condensation unit 300 further comprises a condensation tower 320, wherein a gas phase feeding pipe 321, a gas phase discharging pipe 322 and a condensate return pipe 323 are arranged on the condensation tower 320, the gas phase feeding pipe 321 and the condensate return pipe 323 are connected with the condensation kettle 310, the gas phase discharging pipe 322 is connected with a gas treatment device, gas phase substances generated in the condensation reaction process in the condensation kettle 310 enter the condensation tower 320 through the bottom of the condensation tower 320 for condensation, condensate flows back to the condensation kettle 310 through the condensate return pipe 323, and non-condensable gas is discharged to the gas treatment device through the gas phase discharging pipe 322 for centralized disposal.
Referring to fig. 5, the water washing centrifugal unit 400 receives the condensation reaction solution output from the condensation unit 300, performs multi-stage water washing, and transfers wet carbendazim obtained after the water washing to the drying unit 500.
Specifically, the water washing centrifugal unit 400 includes a water washing tank 410, a belt vacuum filter 420, a carbendazim beating tank 430, and a carbendazim centrifuge 440, which are connected in sequence. The washing tank 410 is filled with washing desalted water, the washing tank 410 is provided with a washing liquid discharge pump 411, the discharge end of the washing liquid discharge pump 411 is connected with the belt vacuum filter 440, at least 2 connection points are arranged in the running direction of the belt vacuum filter 440, the belt vacuum filter 440 receives the carbendazim crude liquid conveyed by the condensation unit 300, and the washing water pumped by the washing liquid discharge pump 411 is washed under the condition of vacuum existence.
After the water washing is completed, the filter cake is transferred to the carbendazim beating tank 430 by the belt vacuum filter 440, and beating is completed in the carbendazim beating tank. A carbendazim slurry discharging pump 431 is arranged on the carbendazim pulping tank 430, and the pulped carbendazim slurry is pumped into the carbendazim centrifuge 440 through the carbendazim slurry discharging pump 431 for centrifugal dehydration to obtain wet carbendazim. And the washing water at the front end of the belt type vacuum filter 440 enters a wastewater pond, and is discharged after wastewater treatment operation.
Further, the water washing centrifugal unit 400 further includes a wet carbendazim conveying device 460 disposed below the discharge port of the carbendazim centrifuge 440, and the wet carbendazim conveying device 460 conveys the wet carbendazim obtained after the centrifugation to the drying unit 500 for drying.
Referring to fig. 6 together, the drying unit 500 receives the wet carbendazim transferred by the water washing centrifugal unit 400 and dries it.
Specifically, the drying unit 500 includes a fluidized bed dryer 510, a cyclone 520, and a bag-type dust collector 530, the fluidized bed dryer 510 receives the wet carbendazim conveyed by the water washing centrifugal unit 400, and contacts with hot air for drying, and the dried carbendazim is discharged through a discharge outlet of the fluidized bed dryer 510, packaged, and transported. The cyclone 520 and the bag-type dust collector 530 are connected in series to the top of the fluidized bed dryer 510, and are configured to collect solid powder discharged from the top of the fluidized bed dryer 510, and collect and discharge tail gas.
Referring to fig. 7, in another embodiment of the present invention, the carbendazim cleaning production system 10 further includes a tail gas absorption unit 600, wherein the tail gas absorption unit 600 includes a draught fan 610, a primary alkaline tower 620 and a secondary alkaline tower 630, which are connected in sequence, and an inlet end of the draught fan 610 is connected to the lime nitrogen hydrolysis unit 100, the amination unit 200, the condensation unit 300, the water washing centrifugal unit 400 and the drying unit 500, respectively, so as to collect tail gas generated in the carbendazim production process, and enable the tail gas to pass through the primary alkaline tower 620 and the secondary alkaline tower 630 for alkaline washing discharge.
Specifically, a primary alkaline washing pump 621 is arranged at the bottom of the primary alkaline washing tower 620, a secondary alkaline washing pump 631 is arranged at the bottom of the secondary alkaline washing tower 630, an outlet end of the induced draft fan 610 is connected to the bottom of the primary alkaline washing tower 620, tail gas generated in the carbendazim production process enters the primary alkaline washing tower 620 through the bottom of the primary alkaline washing tower 620 and is in contact washing with the reflux circulating alkaline liquid pumped by the primary alkaline washing pump 621, the washed tail gas passes through the secondary alkaline washing tower 630 and is in contact washing with the reflux circulating alkaline liquid pumped by the secondary alkaline washing pump 631, and qualified tail gas after secondary washing is discharged.
Referring to fig. 8, in another embodiment of the present invention, the carbendazim cleaning production system 10 further includes a water treatment unit 700, wherein the water treatment unit 700 includes a decolorization device 710, a desalination device 720 and a biochemical reaction tank 730 connected in sequence.
The decoloring device 710 receives the wastewater generated in the production process by the lime nitrogen hydrolysis unit 100, the amination unit 200, the condensation unit 300, the water washing centrifugal unit 400 and the drying unit 500, decolors the wastewater, and transmits the decolored wastewater to the desalting device.
Specifically, the decoloring device 710 is a fenton reaction kettle, and wastewater passes through the decoloring device 710 and undergoes an oxidation reaction with a fenton reaction reagent, so that macromolecular phenazine substances in the wastewater are oxidized and decolored.
The desalting device 720 receives the decolored wastewater delivered by the decoloring device 710, performs desalting treatment on the decolored wastewater, and delivers the desalted wastewater to the biochemical reaction tank 730. Specifically, the desalination device 720 is an MVR evaporator, and the decolorized wastewater is evaporated and concentrated by the desalination device 720, and then filter residue is removed by filter pressing, so that the salt content in the wastewater is reduced. The desalted wastewater enters the biochemical reaction tank 730.
The biochemical reaction tank 730 receives the desalted wastewater conveyed by the desalting device 720, carries out biochemical treatment on the desalted wastewater, reduces indexes such as COD (chemical oxygen demand) and ammonia nitrogen in the wastewater, and conveys qualified wastewater after biochemical treatment to a municipal sewage pipe network.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention.
Claims (9)
1. A carbendazim clean production system is characterized by comprising a lime nitrogen hydrolysis unit, an amination unit, a condensation unit, a water washing centrifugal unit and a drying unit which are sequentially connected;
the lime nitrogen hydrolysis unit receives raw materials of lime nitrogen and sodium carbonate, independently hydrolyzes the lime nitrogen to generate cyanamide, and pumps the cyanamide to the amination unit; the lime nitrogen hydrolysis unit comprises a mixing ground pool, a hydrolysis kettle, a decalcification filter press and a cyanamide intermediate storage tank which are connected in sequence;
the mixing and stirring tank is arranged on the mixing tank, receives the lime nitrogen and sodium carbonate solution, uniformly mixes the lime nitrogen and the sodium carbonate solution under the stirring action of the mixing and stirring tank, and pumps the mixed solution of the lime nitrogen and the sodium carbonate to the hydrolysis kettle;
the hydrolysis kettle receives the mixed liquid of the lime nitrogen and the sodium carbonate pumped by the mixing ground pool, completes the hydrolysis of the lime nitrogen, and conveys the hydrolysate to the decalcification filter press;
the decalcification filter press receives the hydrolysate conveyed by the hydrolysis kettle, performs filter pressing on the hydrolysate, separates cyanamide, and conveys the cyanamide to a cyanamide intermediate storage tank;
the cyanamide intermediate storage tank receives and temporarily stores the cyanamide delivered by the decalcification filter press and pumps the cyanamide to the amination unit;
the amination unit receives cyanamide, methyl chloroformate and liquid caustic soda pumped by the lime nitrogen hydrolysis unit to complete amination reaction and output amination reaction liquid to the condensation unit;
the condensation unit receives the amination reaction liquid output by the amination unit, o-phenylenediamine, hydrochloric acid and formaldehyde to complete condensation reaction, and outputs the condensation reaction liquid to the washing centrifugal unit;
the water washing centrifugal unit receives the condensation reaction liquid output by the condensation unit, carries out multistage water washing, and conveys wet carbendazim obtained after water washing to the drying unit;
the drying unit receives the wet carbendazim conveyed by the water washing centrifugal unit and dries the wet carbendazim.
2. The carbendazim clean production system according to claim 1, wherein the lime nitrogen hydrolysis unit further comprises a residue pulping tank, a secondary filter press and a filtrate tank which are connected in sequence, wherein the pulping tank is connected with a residue outlet of the decalcification filter press;
the pulping tank receives the filter residue from the decalcification filter press, pulps the filter residue, and conveys the slurry to the secondary filter press;
the secondary filter press receives the slurry conveyed by the pulping tank, performs filter pressing on the slurry, conveys filtrate to the filtrate tank, and conveys filter residues to a slag discharge plant;
the filtrate tank receives filtrate from a secondary filter press and pumps the filtrate to the compounding ground pool.
3. The carbendazim clean production system of claim 1, wherein the amination unit comprises an amination kettle, and a methyl chloroformate feeding buffer tank and a caustic soda feeding buffer tank connected with the amination kettle, wherein the methyl chloroformate feeding buffer tank receives methyl chloroformate feeding and adds methyl chloroformate dropwise to the amination kettle, the caustic soda feeding buffer tank receives caustic soda feeding and adds caustic soda liquid dropwise to the amination kettle, the amination kettle receives cyanamide pumped by the hydrolysis unit, the methyl chloroformate added dropwise from the methyl chloroformate feeding buffer tank and the caustic soda liquid added dropwise from the caustic soda feeding buffer tank, completes amination reaction, and outputs amination reaction liquid to the condensation unit.
4. The carbendazim clean production system of claim 3, wherein a weighing module is disposed on the methyl chloroformate feed buffer tank.
5. The carbendazim clean production system of claim 3, wherein a nitrogen feed line is provided on the amination kettle.
6. The carbendazim clean production system of claim 1, wherein the condensation unit comprises a condensation kettle, the condensation kettle receives the amination reaction liquid and hydrochloric acid, o-phenylenediamine and formaldehyde feed materials conveyed by the amination unit, completes condensation reaction, generates crude carbendazim liquid, and conveys the crude carbendazim liquid to the centrifugal water washing unit.
7. The carbendazim cleaning production system as claimed in claim 1, wherein the water washing centrifugal unit comprises a water washing tank, a belt type vacuum filter, a carbendazim beating tank and a carbendazim centrifuge which are connected in sequence, the water washing tank is filled with desalted water for water washing, the belt type vacuum filter receives the crude carbendazim liquid and desalted water which are conveyed by the condensation unit, the water washing of the crude carbendazim liquid is completed under the condition of vacuum, and the washed carbendazim is conveyed into the carbendazim beating tank;
the carbendazim pulping tank receives the carbendazim solid conveyed by the belt vacuum filter, water is added to pulp the carbendazim, and the pulped carbendazim is conveyed to the carbendazim centrifuge;
and the carbendazim centrifuge receives the pulped carbendazim conveyed by the carbendazim pulping tank, performs centrifugal separation to obtain wet carbendazim, and conveys the wet carbendazim to the drying unit.
8. The carbendazim clean-production system of claim 1, further comprising a tail gas absorption unit,
the tail gas absorption unit comprises a draught fan, a primary alkali wash tower and a secondary alkali wash tower which are sequentially connected, wherein the inlet end of the draught fan is respectively connected with the lime nitrogen hydrolysis unit, the amination unit, the condensation unit, the water washing centrifugal unit and the drying unit so as to collect tail gas generated in the carbendazim production process, and the tail gas is subjected to alkali wash discharge sequentially through the primary alkali wash tower and the secondary alkali wash tower.
9. The carbendazim clean production system of claim 1, further comprising a water treatment unit, wherein the water treatment unit comprises a decolorization device, a desalination device and a biochemical reaction tank which are connected in sequence;
the decoloring device is used for respectively receiving wastewater generated in the production process of the lime nitrogen hydrolysis unit, the amination unit, the condensation unit, the water washing centrifugal unit and the drying unit, decoloring the wastewater and conveying the decolored wastewater to the desalting device;
the desalting device receives the decolored wastewater conveyed by the decoloring device, carries out desalting treatment on the decolored wastewater, and conveys the desalted wastewater to the biochemical reaction tank;
and the biochemical reaction tank receives the desalted wastewater conveyed by the desalting device, carries out biochemical treatment on the desalted wastewater, and conveys the biochemically treated wastewater to a municipal sewage pipe network.
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