CN112759163A - Treatment method and treatment system for residual liquid generated in benzoyl chloride production process - Google Patents

Treatment method and treatment system for residual liquid generated in benzoyl chloride production process Download PDF

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CN112759163A
CN112759163A CN202011636531.1A CN202011636531A CN112759163A CN 112759163 A CN112759163 A CN 112759163A CN 202011636531 A CN202011636531 A CN 202011636531A CN 112759163 A CN112759163 A CN 112759163A
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hydrolysis
residual liquid
flue gas
incineration
treatment
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陈福泰
褚永前
杨艳
白立强
高锐军
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Go Higher Environment Group Co ltd
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Go Higher Environment Group Co ltd
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    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
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Abstract

The application belongs to the technical field of hazardous waste treatment, and particularly discloses a treatment method of residual liquid generated in a benzoyl chloride production process, which mainly comprises the steps of hydrolysis dechlorination, cooling solidification, incineration and the like. The application has at least one of the following beneficial effects: the method adopts a disposal mode of firstly carrying out hydrolysis dechlorination and then thoroughly burning, so that the corrosion risk to equipment is reduced; the residual liquid is converted into solid waste impurities, so that the transportation and incineration of the feed are facilitated, the blockage of the liquid feed is avoided, and the cleaning maintenance is reduced; after high-temperature incineration, the flue gas is discharged to EU 2000 standard after reaching the standard through a flue gas treatment system, and completely harmless treatment can be realized; the main components in the ash content are fly ash and incineration ash slag collected in each dust removal stage, the residue content is low, and the fly ash and the incineration ash slag can be directly and safely buried; more than 99.9 percent of chlorine in the residual liquid after dechlorination is removed through hydrolysis, so that a large amount of acid gas generated by direct burning is avoided, the deacidification load of flue gas treatment is effectively reduced, and the tail gas treatment is easier to reach the standard.

Description

Treatment method and treatment system for residual liquid generated in benzoyl chloride production process
Technical Field
The application belongs to the technical field of hazardous waste treatment, and particularly relates to a treatment method and a treatment system for residual liquid generated in a benzoyl chloride preparation process.
Background
Benzoyl chloride, a colorless liquid, has an irritating odor. Dissolved in ether, chloroform and benzene. Benzoyl chloride is a raw material for organic synthesis, dyes and medicine production, and is mainly used for preparing initiators of dibenzoyl peroxide, tert-butyl peroxybenzoate, pesticide herbicides and the like. The synthesis process of benzoyl chloride mainly comprises a toluene method, a phosgene method, a benzoic acid silicon tetrachloride method and the like, and due to the influence of raw materials and the synthesis process, a large amount of benzoyl chloride and other toxic and harmful substances are still contained in distillation residual liquid generated in the production process of benzoyl chloride, so that the benzoyl chloride has strong pungent smell, is greatly harmful to the environment and human health after being directly discharged, and needs to be reasonably and safely disposed.
Disclosure of Invention
In the prior art, one of the methods for treating the residual liquid is direct incineration treatment, and the method has the disadvantages of serious corrosion to incineration equipment, frequent equipment cleaning and reduced service life due to higher chlorine content in the residual liquid; the other method is to convert benzoyl chloride in the residual liquid into products such as benzoic acid and the like for recovery by methods such as distillation, synthesis and the like, but the method has complex process and has the problems of low recovery purity, difficult utilization, large amount of residues after treatment, further treatment and the like.
Patent CN108191641A discloses a benzoyl chloride recovery treatment method, which comprises the steps of firstly carrying out vacuum distillation treatment on benzoyl chloride residual liquid, condensing to recover benzoyl chloride, and secondly carrying out alkaline hydrolysis treatment on the residual benzoyl chloride residual liquid to obtain treatment residues; the recovery rate of the process is about 50 percent, the process is only suitable for treating residual liquid with less impurities, and the residual 50 percent of residues are required to be further treated.
Based on the method, the method for treating the residual liquid generated in the production process of the benzoyl chloride is simple in process, good in treatment effect, small in equipment corrosion and capable of completely realizing harmless treatment.
The application is realized by the following scheme:
the application provides a treatment method of residual liquid generated in a benzoyl chloride production process, which comprises the following steps:
s1: hydrolysis and dechlorination: heating the residual liquid to over 125 ℃, and slowly dripping a hydrolytic agent for hydrolysis;
s2: cooling and solidifying: after the hydrolysis is finished, directly discharging the hydrolyzed product, naturally cooling and solidifying;
s3: and (3) incineration: the product cured in step S2 is incinerated.
This application is through the processing mode of antichloration burning again earlier, but greatly reduced contains chlorine waste and burns the corruption to equipment, reduces the clearance number of times, improves service life.
The hydrolysis reaction formula of the hydrolysis dechlorination in the application is abbreviated as follows:
C6H5COCl +H2O = C6H5COOH +HCl
in the application, the benzene formyl chloride which is not extracted in the production process of the benzene formyl chloride is converted into benzoic acid and hydrogen chloride through hydrolysis, and the hydrogen chloride gas forms salt water after being absorbed by alkali liquor and enters a sewage treatment system without causing any influence on the environment; benzoic acid, as well as other materials in the raffinate, are converted to water and carbon dioxide by high temperature incineration.
In the application, as the melting point of the benzoic acid is 122 ℃, the benzoic acid is selectively heated to more than 125 ℃ for hydrolysis, so that the benzoic acid exists in the reactor in a liquid form, and the influence on the hydrolysis reaction due to the solidification of the benzoic acid is avoided.
In one embodiment of the present application, the raffinate is heated to 125 ℃ to 150 ℃, e.g., to 125 ℃, 130 ℃, 132 ℃, 135 ℃, 138 ℃, 140 ℃, 142 ℃, 145 ℃, 150 ℃, etc.
In one embodiment of the present application, the hydrolytic dechlorination is performed under negative pressure.
In one embodiment of the present application, the negative pressure is 10-20 kpa.
Because the energy consumption of the hydrolysis dechlorination heating process and the negative pressure providing engineering is large, the hydrolysis dechlorination is carried out under the condition that the residual liquid is heated to 130-140 ℃ and the negative pressure is 10-20kpa on the basis of balancing the energy consumption of heating and negative pressure and influencing the hydrolysis process. More preferably, the hydrolysis dechlorination is carried out under the condition that the residual liquid is heated to 135 ℃ and the negative pressure is 15kpa, and the condition can reduce energy consumption and cost as much as possible under the condition of ensuring the normal running of the hydrolysis reaction.
In one embodiment of the present application, the hydrolyzing agent is water or lye. The alkali liquor is used as a hydrolytic agent instead of water, and can absorb a part of hydrogen chloride gas, so that the concentration of reaction products is reduced, and the hydrolytic conversion rate is increased. The concentration and type of the alkali solution are not limited in this application, and may be, for example, NaOH solution, KOH solution, etc.
In a specific embodiment of this application, the flue gas that burns adopts the mode treatment of second grade denitration + second grade deacidification + second grade dust removal, adopts dry-type deacidification, bag-type dust removal, wet process deacidification, SNCR denitration, ozone denitration, wet electric dust removal's technology combination to carry out purification treatment to the flue gas promptly to guarantee that the flue gas is up to standard and discharges.
In one embodiment of the present application, the raffinate is the raffinate produced in the hydrolysis of trichlorotoluene and benzoic acid to benzoyl chloride.
The main components in the residual liquid comprise unreacted trichlorotoluene, benzoyl chloride, benzoic acid, benzoic anhydride, tar polymer and the like. And unreacted trichlorotoluene can be converted into benzoic acid and hydrogen chloride through hydrolysis, so that the trichlorotoluene is removed.
In one embodiment of the present application, the hydrogen chloride produced by the hydrolytic dechlorination is absorbed by a hydrogen chloride absorption unit.
In one embodiment of the present application, the hydrogen chloride absorbing device is a spray tower.
The application also provides a processing system of raffinate that produces in benzoyl chloride production process, includes:
the adjusting tank is used for adjusting the homogenization and the average amount of the residual liquid;
the hydrolysis reactor is used for the hydrolysis reaction of the residual liquid;
an intermediate container for collecting solid residue generated by hydrolysis reaction;
the hydrogen chloride absorption device is used for absorbing hydrogen chloride gas generated by hydrolysis reaction;
the hazardous waste incinerator is used for incinerating the hydrolyzed solid residues;
the flue gas purification device is used for purifying flue gas generated after incineration;
the adjusting tank, the hydrolysis reactor, the intermediate container, the hazardous waste incinerator and the flue gas purification device are sequentially connected, and the hydrogen chloride absorption device is connected with the hydrolysis reactor through a pipeline.
In a specific embodiment of this application, flue gas purification device includes SNCR denitrification facility, quench tower, dry-type deacidification device, sack cleaner, ozone denitrification facility, wet process deacidification tower and wet electric precipitator who connects gradually.
The method and the device for treating the residual liquid generated in the production process of the benzoyl chloride have at least one of the following beneficial effects:
firstly, the treatment method of the residual liquid generated in the production process of benzoyl chloride adopts a treatment mode of firstly performing hydrolysis dechlorination and then completely burning, reduces the corrosion risk to equipment, and can realize completely harmless treatment.
Secondly, converting the residual liquid into solid waste impurities, which is convenient for transportation and incineration feeding; in addition, liquid feeding generally needs to be sprayed into the incinerator through spray guns and other modes, equipment is complex, a feeding hole is easy to block, cleaning and maintenance are frequent, and the problem can be effectively avoided after the liquid feeding is converted into solid feeding.
And thirdly, after high-temperature incineration, the organic matters are converted into water and carbon dioxide, and the flue gas is discharged to EU 2000 standard after reaching the standard through a flue gas treatment system, so that completely harmless treatment can be realized.
And fourthly, the main components in the ash content are fly ash and incineration ash slag collected in each dust removal stage, the residue content is low, the fly ash and the incineration ash slag mainly comprise calcium hydroxide, sodium chloride and the like used or generated in the flue gas treatment, and the fly ash and the incineration ash slag can be directly and safely buried.
And fifthly, after dechlorination treatment of the residual liquid, over 99.9 percent of chlorine is removed through hydrolysis, so that a large amount of acid gas generated by direct burning is avoided, the deacidification load of flue gas treatment is effectively reduced, and the tail gas treatment is easier to reach the standard.
Drawings
FIG. 1 is a system diagram of the raffinate treatment provided in this example.
Fig. 2 is a process flow diagram of the incineration system provided in the present example.
Detailed Description
Some, but not all embodiments of the invention are described. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
Example 1 treatment System for raffinate produced in benzoyl chloride production Process
FIG. 1 is a system diagram of the raffinate treatment provided in this example. As shown in FIG. 1, the system for treating the raffinate produced in the production of benzoyl chloride comprises: the device comprises an adjusting tank for homogenizing and uniform adjustment of residual liquid, a hydrolysis reactor for residual liquid hydrolysis reaction, an intermediate container for collecting solid residues generated by hydrolysis reaction, a hydrogen chloride absorption device for absorbing hydrogen chloride gas generated by hydrolysis reaction, a hazardous waste incinerator for incineration disposal of the hydrolyzed solid residues, and a flue gas purification device for purification treatment of flue gas generated after incineration. The adjusting tank, the hydrolysis reactor, the intermediate container, the hazardous waste incinerator and the flue gas purification device are sequentially connected through a pipeline, and the hydrogen chloride absorption device is connected with the hydrolysis reactor through a pipeline.
EXAMPLE 2 method for treating raffinate produced in the production of benzoyl chloride
In this example, the residual liquid generated in the process of generating benzoyl chloride by hydrolysis reaction of trichlorotoluene and benzoic acid, whose main components include benzoyl chloride, benzoic acid, benzoic anhydride, tar polymer, etc., and whose total chlorine content is 12.23%, was treated by the treatment system shown in fig. 1. The processing method comprises the following steps:
s1: hydrolysis and dechlorination:
collecting the residual liquid, storing in a homogenizing and quantity-balancing adjusting tank, and homogenizing and quantity-balancing adjusting to homogenize the raw material; and (3) conveying the homogenized residual liquid into a hydrolysis reactor, heating to 135 ℃, keeping the negative pressure of the hydrolysis reactor at 15kpa, slowly dripping water, starting stirring, and performing the following hydrolysis reaction on benzoyl chloride in the residual liquid:
C6H5COCl +H2O = C6H5COOH +HCl
at the moment, the hydrolysis reactor can generate fog-like hydrogen chloride gas which is discharged through an exhaust port of the hydrolysis reactor and enters a hydrogen chloride absorption device; and (4) continuously observing along with the addition of water, and determining that the hydrolysis reaction is finished when no fog-shaped hydrogen chloride gas is generated in the hydrolysis reactor.
In this embodiment, when the residual liquid is reacted, the higher the temperature is, the faster the reaction is, the higher the negative pressure is, the faster the reaction is, the reaction temperature may be 125 ℃ or more, for example, between 125 ℃ and 150 ℃, and the negative pressure is 10 to 20kpa, but considering that a large amount of energy is consumed for heating the residual liquid and maintaining the negative pressure, the inventors of the present application finally determined to maintain the negative pressure of the hydrolysis reactor at 15kpa and control the reaction temperature between 130 ℃ and 140 ℃ by testing the relationship between the reaction rate, the time required for the reaction, and the energy consumption cost under different temperature conditions and different negative pressure conditions. The reaction temperature in this example was 135 ℃.
In the embodiment, the alkali liquor can be slowly dripped to serve as the hydrolytic agent, and the concentration of the reaction product is reduced because the alkali liquor can react with the hydrogen chloride of the reaction product, which is more beneficial to the hydrolysis reaction. The alkali liquor can be 10% -20% sodium hydroxide solution.
In this example, even if the starting material contains unreacted trichlorotoluene, the starting material can be hydrolyzed into benzoic acid and hydrogen chloride.
The hydrogen chloride absorption device in the embodiment adopts a spray tower, and utilizes a 20% NaOH solution to absorb hydrogen chloride. After hydrolysis dechlorination treatment, the total chlorine content is less than 0.01 percent.
S2: cooling and solidifying:
introducing reaction residual liquid (benzoic acid, tar polymer and the like) in the hydrolysis reactor into an intermediate container, naturally cooling, solidifying the residual liquid, cooling to a normal-temperature solid state, forming dangerous waste, and sending the dangerous waste to an incineration system for treatment;
s3: high-temperature incineration:
the hazardous waste is sent into a hazardous waste incinerator for incineration disposal, so that thorough harmless treatment is realized.
According to the requirements of the "dangerous waste and medical waste disposal facility construction project review outline (trial implementation)", in order to remove harmful components in the flue gas to the maximum extent, achieve the best effect, save investment and reduce operating cost, in the embodiment, the flue gas of the incineration system adopts three levels: and (2) performing secondary denitration, secondary deacidification and secondary dedusting, namely performing purification treatment on the flue gas by adopting the process combination of dry deacidification, bag type dedusting, wet deacidification, SNCR denitration, ozone denitration, wet electric dedusting and the like so as to ensure that the flue gas is discharged up to the standard.
The second-stage denitration in this embodiment includes:
the first stage is SNCR denitration. A denitrification reaction system is arranged on the membrane wall boiler. The urea solution after being configured is lifted by an atomizing pump to enter a nozzle, the nozzle is atomized and sprayed into the waste heat boiler by pressure, the smoke and the sprayed atomized urea solution are fully mixed under the environment of 800 plus materials at 1000 ℃, and NOx components in the smoke are in O2In the presence of the urea, the urea solution and the urea are subjected to reduction reaction, and meanwhile, the moisture of the urea solution is completely vaporized and taken away by the flue gas.
The second stage is ozone denitration, a flue behind the bag-type dust remover is selected, and holes are formed in the flue to perform ozone injection. The generated ozone is sent into an ozone special injection system and is injected into a flue through an ozone injection grid so as to ensure the full mixing reaction of the ozone and the flue gas. SO is carried out on nitrogen oxides (high valence nitrogen oxides) generated by reaction through wet deacidification2And NO2So as to achieve the aim of denitration.
The secondary deacidification in this example includes:
the first stage is dry deacidification, and the flue gas reacts with sprayed slaked lime in a dry deacidification tower to absorb acid gas for primary deacidification.
The second stage is wet deacidification. The washing deacidification tower adopts liquid caustic soda to neutralize and absorb acid gas (SO) in the flue gas2HCl, HF). The alkali liquor is maintained at a certain pH value, and is circulated by a circulating pump. Alkali liquor passes through an alkali liquor pumpAdding the mixture into an inlet pipeline of an inlet circulating pump. The addition amount of the alkali liquor is controlled by the pH value of the circulating alkali liquor. And a pH meter monitors the alkali concentration of the washing water on line and controls the amount of the added liquid medicine so as to ensure the requirement of the circulating liquid on the alkali concentration. The washing water flows out of the washing tower and then enters the washing water tank by gravity, and the washing water is pumped into the washing tower for recycling after the pH value is adjusted. Periodically draining part of the washing water to the pre-cooling water tank, and simultaneously replenishing new washing water to maintain the liquid level of the washing water tank. After the absorption liquid is recycled, the acid gas is washed to be changed into salt which is dissolved in water, the concentration of salt in the absorption liquid is higher and higher, and the design of continuous discharge is adopted.
In this embodiment, the deacidification efficiency can be improved to more than 99% by two-stage deacidification.
The secondary dust removal in the embodiment includes bag dust removal and wet electric dust removal.
The bag-type dust collector filters dust-containing gas by utilizing the filtering action of the fiber fabric, and after the dust-containing gas enters the bag-type dust collector, dust with large particles and large specific gravity falls into the dust hopper due to the sedimentation of the gravity, and the dust is blocked when the gas containing fine dust passes through the filter material, so that the gas is purified.
Wet electric dust removal is high-efficiency gas-liquid separation wet equipment, and micron and submicron particles in flue gas after wet deacidification are collected, so that acid mist at a purification outlet reaches relevant emission indexes. Firstly, a direct-current high-voltage power is input into an electric field, so that corona polar lines of the electric field continuously emit electrons, and gas between electrodes is ionized into positive ions and negative ions. Particles such as dust and acid mist collide with electrons to generate charges. According to the principle that like charges repel and opposite charges attract, the charged dust and acid mist move to the electrodes with opposite electric polarities. The positive ions move to the corona electrode, the negative ions and the electrons move to the precipitation electrode, the charges are transferred to the precipitation electrode, and the acid mist particles losing the charges flow to the bottom of the electric dust (mist) remover along the inner wall of the precipitation electrode by means of dead weight, so that the purposes of removing dust and mist are achieved.
The inlet of the wet electric dust collector is provided with a perforated plate or other flow equalizing devices so that the flue gas can uniformly flow through the electric field; the shell is sealed, and leakage cannot occur; the design of the shell avoids dead corners or plaster accumulation areas as much as possible, and the top of the shell is free from water accumulation, so that the shell is ensured not to deform after long-term operation; a manhole door should be provided to allow for measures such as inspection of the internal components.
The flue gas generated by the incineration of the hazardous waste incinerator in the embodiment is treated by the flue gas purification device, and the process flow is shown in fig. 2.
As shown in fig. 2, the flue gas is firstly subjected to primary denitration (SNCR denitration), 50% urea solution is added, and primary denitration of the flue gas is performed at 800 ℃; the gas after the primary denitration enters a quenching tower, the temperature is reduced to be below 200 ℃, and the generation of dioxin is prevented; then entering a first-stage deacidification (dry deacidification), and spraying slaked lime powder to absorb part of acid gas at the temperature of 180-190 ℃; the gas after the primary deacidification enters primary dust removal (bag type dust removal) for filtration and dust removal; then, performing two-stage denitration (ozone denitration), and performing denitration by using 10% of ozone at the temperature of 170-180 ℃; and (3) the gas after the secondary denitration enters a secondary deacidification (wet deacidification), 20% NaOH solution is sprayed into a wet deacidification tower at the temperature of 140 ℃, acidity and harmful substances are removed, and the gas is finally subjected to secondary dedusting (wet electric dedusting) and is discharged after reaching the standard.
In the embodiment, after the residual liquid is incinerated at high temperature, organic matters are converted into water and carbon dioxide, and the flue gas is discharged to EU 2000 flue gas emission standard after reaching the standard through a flue gas treatment system, so that completely harmless treatment can be realized.
The dust in the embodiment is mainly fly ash and incineration ash collected in each dust removal stage, and the collected dust components are mainly calcium hydroxide, sodium chloride and the like used or generated in the flue gas treatment, so that the fly ash and the incineration ash can be safely buried.
Finally, the residual liquid treatment method in the production process of benzoyl chloride provided by the application has the advantages that after hydrolysis and dechlorination, the chlorine content is lower than 0.01%, the corrosion of incineration to equipment can be greatly reduced, the cleaning frequency is reduced, the service life of the equipment is prolonged, harmless treatment can be completely realized, the process is simple, the operation is convenient, and the method has wide market application value.
The present embodiment is only for explaining the present application, and it is not limited to the present application, and those skilled in the art can make modifications of the present embodiment without inventive contribution as needed after reading the present specification, but all of them are protected by patent law within the scope of the claims of the present application.

Claims (10)

1. A method for treating residual liquid generated in the production process of benzoyl chloride is characterized by comprising the following steps:
s1: hydrolysis and dechlorination: heating the residual liquid to over 125 ℃, and slowly dripping a hydrolytic agent for hydrolysis;
s2: cooling and solidifying: after the hydrolysis is finished, directly discharging the hydrolyzed product, naturally cooling and solidifying;
s3: and (3) incineration: the product cured in step S2 is incinerated.
2. The process according to claim 1, characterized in that the raffinate is heated to a temperature of 125 ℃ to 150 ℃.
3. The process according to claim 1, wherein the raffinate is heated to a temperature of 130 ℃ to 140 ℃.
4. The process according to claim 1, characterized in that the hydrolytic dechlorination is carried out at a negative pressure of 10-20 kpa.
5. The process of claim 1, wherein the hydrolyzing agent is water or lye.
6. The treatment method according to claim 1, wherein the incineration flue gas is treated by using dry deacidification, bag dedusting, wet deacidification, SNCR denitration, ozone denitration and wet electric dust removal processes.
7. The process of claim 1, wherein the raffinate is a raffinate from a process in which trichlorotoluene and benzoic acid are hydrolyzed to benzoyl chloride.
8. The process according to any one of claims 1 to 7, characterized in that the hydrogen chloride produced by the hydrolytic dechlorination is absorbed by a spray tower.
9. Processing system of raffinate that produces in benzoyl chloride production process, its characterized in that includes:
the adjusting tank is used for adjusting the homogenization and the average amount of the residual liquid;
the hydrolysis reactor is used for the hydrolysis reaction of the residual liquid;
an intermediate container for collecting solid residue generated by hydrolysis reaction;
the hydrogen chloride absorption device is used for absorbing hydrogen chloride gas generated by hydrolysis reaction;
the hazardous waste incinerator is used for incinerating the hydrolyzed solid residues;
the flue gas purification device is used for purifying flue gas generated after incineration;
the adjusting tank, the hydrolysis reactor, the intermediate container, the hazardous waste incinerator and the flue gas purification device are sequentially connected, and the hydrogen chloride absorption device is connected with the hydrolysis reactor through a pipeline.
10. The treatment system according to claim 9, wherein the flue gas purification device comprises an SNCR (selective non-catalytic reduction) denitration device, a quench tower, a dry deacidification device, a bag-type dust remover, an ozone denitration device, a wet deacidification tower and a wet electric dust remover which are connected in sequence.
CN202011636531.1A 2020-12-31 2020-12-31 Treatment method and treatment system for residual liquid generated in benzoyl chloride production process Pending CN112759163A (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114477588A (en) * 2022-01-26 2022-05-13 海宁天纵电子科技有限公司 Liquid medicine destroying device with automatic detection function
WO2023061624A1 (en) * 2021-10-12 2023-04-20 Linde Gmbh Method for reducing the content of nitrogen oxides in a flue gas stream of thermal waste treatment plants

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CN103787874A (en) * 2014-02-28 2014-05-14 宜都市友源实业有限公司 Preparation process of benzoyl chloride
CN108191641A (en) * 2018-01-08 2018-06-22 沾化鹏辉化工有限公司 A kind of recovery and treatment method of chlorobenzoyl chloride raffinate
CN212188526U (en) * 2019-12-24 2020-12-22 惠州Tcl环境科技有限公司 Flue gas treatment system after sludge treatment

Patent Citations (3)

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Publication number Priority date Publication date Assignee Title
CN103787874A (en) * 2014-02-28 2014-05-14 宜都市友源实业有限公司 Preparation process of benzoyl chloride
CN108191641A (en) * 2018-01-08 2018-06-22 沾化鹏辉化工有限公司 A kind of recovery and treatment method of chlorobenzoyl chloride raffinate
CN212188526U (en) * 2019-12-24 2020-12-22 惠州Tcl环境科技有限公司 Flue gas treatment system after sludge treatment

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023061624A1 (en) * 2021-10-12 2023-04-20 Linde Gmbh Method for reducing the content of nitrogen oxides in a flue gas stream of thermal waste treatment plants
CN114477588A (en) * 2022-01-26 2022-05-13 海宁天纵电子科技有限公司 Liquid medicine destroying device with automatic detection function
CN114477588B (en) * 2022-01-26 2023-11-14 海宁天纵电子科技有限公司 Liquid medicine destroying device with automatic detection function

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