CN102718623A - Method of producing methane chloride by using byproduct hydrogen chloride of tetrachloroethylene device - Google Patents
Method of producing methane chloride by using byproduct hydrogen chloride of tetrachloroethylene device Download PDFInfo
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- CN102718623A CN102718623A CN2012102433060A CN201210243306A CN102718623A CN 102718623 A CN102718623 A CN 102718623A CN 2012102433060 A CN2012102433060 A CN 2012102433060A CN 201210243306 A CN201210243306 A CN 201210243306A CN 102718623 A CN102718623 A CN 102718623A
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Abstract
The invention provides a method for producing methane chloride by using byproduct hydrogen chloride of a tetrachloroethylene device. The method comprises the steps of: (a) condensing the byproduct hydrogen chloride of the gaseous raw material tetrachloroethylene device, and separating to remove the liquid-phase impurities so as to obtain gas-phase hydrogen chloride, wherein a condensing outlet is at temperature of 40 DEG C; (b) heating the hydrogen chloride obtained by purifying in the step (a) to reach the temperature of 100 to 120 DEG C, and mixing with the carbinol at 100 to 120 DEG C from a carbinol evaporator (4) according to the volume ratio of 1.2: 1, and then introducing the mixture into a reactor (6), and reacting in the presence of 50-80% zinc chloride solution to produce methane chloride; and (c) quickly moving the reactive gas-phase component prepared in step (b) out of the reactor (6), and sequentially processing the reactive gas-phase component by condensing, washing with water, neutralizing with alkaline liquor, drying with vitriol, compressing, and then processing through a rectifying column (11). The method provided by the invention is efficient, simple, and fully utilizes the chloride resource.
Description
Technical field
The present invention relates to a kind of preparation method of monochloro methane, be specifically related to a kind of method of utilizing zellon device by-product hydrogen chloride to produce monochloro methane.
Background technology
Monochloro methane purposes in industry is extremely extensive, is mainly used in fields such as synthesizing organo-silicon, methylene dichloride, trichloromethane, zellon, methylcellulose gum, pharmacy.
Monochloro methane also can be used as the raw material of synthesizing methane muriate, organosilicon and zellon, and it is the industrialized unit of the synthetic zellon of raw material that present vast and boundless Hua Honghe chemical industry Ltd and Zhejiang Quhuafu Chemical Co., Ltd have with monochloro methane, chlorine, tetracol phenixin.Because HCFC-22 (difluorochloromethane) is equally as ODS; To progressively eliminate from 2013 and restriction is used for refrigeration agent; Therefore novel refrigerant raw material HFC-125 (pentafluoride ethane) is in the stage of rising gradually in the demand of developed countries such as America and Europe at present; Zellon is as the important source material of synthetic HFC-125, and present demand is tending towards vigorous, and market outlook are good.As the raw material monochloro methane of synthetic zellon, will be paid close attention to by enterprise inside the circle more.
And, present methane chloride (methylene dichloride and trichloromethane) and organosilicon production capacity cumulative year after year, the quality and the economic and technical norms of raw material monochloro methane also will be paid close attention in the industry more.
Mentioned method among the Chinese patent CN102019157A with ammonium chloride and synthetic monochloro methane of methyl alcohol catalysis and ammonia; It obtains monochloro methane through gas solid separation, reaction, separation; But this patented technology does not still drop into industrial applications at present, and its technological maturity remains the check of time.
Chinese patent CN101921166A has mentioned the liquid phase production technology for preparing monochloro methane with tetracol phenixin and methyl alcohol.This method is the synthetic monochloro methane of raw material with methyl alcohol, tetracol phenixin, hydrogenchloride; Employing liquid-phase catalysis technology; Temperature of reaction is between 110-180 ℃; Pressure is kept 0.1-0.30MPa, and the reactor outlet mixture is washed, made monochloro methane behind dry, the compression condensation through condensation, gas-liquid separation, scale.Problems such as this method exists catalyst life short, and corrosion of equipment is serious.
It is the method for raw material production monochloro methane with Hydrogen chloride and methyl alcohol that Chinese patent CN101440015 discloses a kind of; Mass concentration is that the Hydrogen chloride of 15-22% and the calcium chloride solution of 40-52% get into the hydrochloric acid Analytic Tower after mixer mixing; Under the broken effect of boiling of calcium chloride; Hydrochloric acid soln is broken azeotropic point, and hydrogen chloride gas is overflowed from the Analytic Tower cat head, rare calcium chloride solution 125-145 ℃ with 0.02-0.1MPa under remove moisture; Methyl alcohol after compressed hydrogen chloride gas and the vaporization gets into reactor drum through after the heater heats, generates the mixture of monochloro methane, methane, monochloroethane, methylene dichloride at the reactor drum internal reaction; The mixture that generates gets into chiller, and after Quench was separated, gas phase got into the sulfuric acid dehumidification system, makes monochloro methane after the compression.The advantage of this method is to utilize lower hydrochloric acid of concentration and the synthetic monochloro methane of methyl alcohol, and shortcoming is that synthetic monochloro methane quality is low, and purity is merely 99.84%, is not suitable for the raw material of downstream organosilicon and methane chloride, is difficult to sell in market.
Chinese patent CN1347862A discloses a kind of in the presence of high-efficiency activated catalyzer; Mol ratio is 1: 1.02～1.1; The methyl alcohol and the hydrogenchloride that are heated to more than 200 ℃ get into the reactor drum internal reaction, and temperature of reaction is 240 ℃～300 ℃, and reaction pressure is 0～0.5MpaG; Reaction times is 4～6 seconds, and the monochloro methane of generation and unconverted anhydrous hydrogen chloride make monochloro methane through washing, alkali cleaning and sulfuric acid drying.This method conversion of methanol is greater than 98%, and the monochloro methane selectivity is greater than 98%, and the work-ing life of catalyzer was at 7500 to 8400 hours.The characteristics of this method are that transformation efficiency is high, selectivity is good, but that shortcoming is a catalyst life is limited, need to change once in 1 year; The domestic catalyst life cycle is short at present; The catalyzer that can satisfy the LP use needs from company's imports such as U.S. Si Tuofu, and the expense of buying catalyzer is high, and procurement cycle is long.This technology needs raw material hydrogenchloride and methyl alcohol are heated to more than 200 ℃ simultaneously, needs supporting heat-conducting oil system, has increased facility investment and working cost.
Chinese patent CN1686981A has announced a kind of under the active catalyst existence condition; With hydrogenchloride and methyl alcohol is raw material; Temperature of reaction is between 260-320 ℃; Between the reaction pressure 0.2-0.6MpaG, gas-phase reaction generates monochloro methane and water, makes monochloro methane through over-quenching, sulfuric acid drying, compression condensation.The advantage of this method is that transformation efficiency is high; But it is high to exist the Gas-phase reactor material to require, and big to equipment corrosion, the temperature of reactor height causes temperature stress to damage appurtenances easily; Exist the easy carbon distribution of catalyzer to cause work-ing life short simultaneously; And owing to do not wash and caustic wash process, cause the equipment corrosion in monochloro methane and the condensation operation big easily, increased the ME cost.
Chinese patent CN 1515528A has announced the novel process that monochloro methane is produced in a kind of liquid catalytic pressurization; This method with hydrogenchloride and methyl alcohol proportional mixing after; In the tank reactor of catalyzer is housed, be 0.05-0.25Mpa in reaction pressure, temperature of reaction is a synthetic monochloro methane under 140-170 ℃ the condition; The material that utilizes pump will participate in reaction is simultaneously realized extracorporeal circulation, prolongs the work-ing life of reaction kettle.Reacted material obtains liquid monochloro methane product through peracid/washing behind vitriol oil washing, the compression condensation.The advantage of this method is that transformation efficiency is high, and catalyzer obtains easily and be cheap, and shortcoming is that this method reaction pressure is high, has been up to 0.25Mpa, and high to equipment requirements, this method has increased dealcoholize column simultaneously, thereby, increased fixed investment and running cost.This method is not clearly put down in writing scope to the concentration and the addition of catalyzer liquor zinci chloridi simultaneously; Be unfavorable for instructing and produce; And the temperature of reaction of this method is too high, has been up to 170 ℃, and at present domestic nonmetal equipment of lining and pipeline are difficult to satisfy the requirement up to 170 ℃; Need or adopt enamel equipment and pipeline from external import lining equipment and pipeline, and the external import lining equipment of import and pipeline or to adopt enamel equipment and pipeline buying expenses be 4-5 times of conventional lining equipment.
Therefore, need provide a kind of method of utilizing zellon device byproduct hydrogen chloride production monochloro methane to address the above problem.
Summary of the invention
The purpose of this invention is to provide and a kind ofly realize that large-scale industry is combined to the method for high-quality monochloro methane, and raw material wherein is from the hydrogenchloride of zellon device by-product.
For realizing foregoing invention purpose of the present invention, the present invention has adopted following technical proposals.
A kind of method of utilizing zellon device by-product hydrogen chloride to produce monochloro methane of the present invention comprises:
(a) purification zellon device byproduct hydrogen chloride: will be gasiform zellon device byproduct hydrogen chloride through 1 condensation of first condensing surface; Get into then and separate liquid phase impurity in the vapour liquid separator 2; Get gas phase hydrogenchloride, wherein said first condensing surface, 1 temperature out is 40 ℃;
(b) preparation monochloro methane: the hydrogenchloride that obtains purifying in the step (a) adopts well heater 3 to be heated to 100 ℃-120 ℃; Be to introduce reactor drum 6 after the mixed of 1.2:1 with the volume ratio from 100 ℃-120 ℃ methyl alcohol of methanol evaporator 4 through mixing device 5; And be to react the generation monochloro methane under the liquor zinci chloridi condition of 50-80% in concentration; The addition of said liquor zinci chloridi is said reactor drum 6 volumetrical 50-80%; Said temperature of reaction is 110 ℃-130 ℃, and pressure is 0.01Mpa-0.03Mpa (gauge pressure), and the residence time is 15-40s;
(c) refining: that the reaction gas phase component of gained in the step (b) is promptly shifted out said reactor drum 6; Successively through 7 condensations of second condensing surface, water wash column 8 washings, the neutralization of soda-wash tower 9 alkali lye, pickling tower 10 sulfuric acid drying, compression, rectifying tower 11, obtain monochloro methane again.
The industrialization production method that utilizes zellon device byproduct hydrogen chloride to produce monochloro methane disclosed by the invention is that zellon device by-product hydrogen chloride is got into reactor drum 6 production monochloro methanes as raw material and methanol mixed after making with extra care impurity.Wherein the temperature of raw material zellon device byproduct hydrogen chloride is 170 ℃.
Several big important factor of influence reaction is: the ratio of the impurity in hydrogenchloride purity, the hydrogenchloride, hydrogenchloride and methyl alcohol, temperature of reactor, catalyst concn, reaction pressure, reaction time.
Byproduct hydrogen chloride from the zellon device contains impurity; This impurity is mainly organochlorine compound; Like tetracol phenixin and zellon etc., tetracol phenixin and zellon at high temperature will be hydrolyzed into impurity effect monochloro methane quality producies such as formaldehyde and formic acid with water generation chemical reaction, and the existence of these impurity exerts an influence to reaction; Taken the volume of reactor drum, the ability of reactor drum can not be fully played.
Vapour liquid separator 2 in the step of the present invention (a) must guarantee that enough separated spaces are to separate liquid state organics; The flow velocity of process gas in vapour liquid separator 2 should be not too high simultaneously, and the flow rate control of gas in vapour liquid separator 2 is advisable between 0.1-0.3m/s.The length-to-diameter ratio of vapour liquid separator 2 is advisable between 2-4, and length-to-diameter ratio helps separating more greatly more, will increase facility investment but increase length-to-diameter ratio.The volume of vapour liquid separator 2 can depend on the circumstances according to the separation task.Processing through step (a) can obtain highly purified hydrogenchloride, and the purity of hydrogenchloride reaches more than 99.9%.
The volume ratio of hydrogenchloride and methyl alcohol helps methyl alcohol is reacted completely more greatly more, but volume ratio is low more to usage ratio of equipment more greatly, and best volume ratio is 1.2:1.
The height of temperature of reaction can determine conversion of methanol, selectivity.Reaction temperature is spent low, and conversion of methanol is low, and speed of reaction is slow, and methyl alcohol does not also have fully reaction just to be taken out of reactor drum 6; Temperature of reaction is too high, and the by product dme of generation is also just more.
Catalyst concn and catalyzer height can influence the generation of monochloro methane equally.The addition of catalyzer liquor zinci chloridi is only relevant with the height of catalyzer in reactor drum, does not have necessary relation with the hydrogenchloride of participating in reaction and the amount of methyl alcohol.Catalyst concn can not be low excessively, otherwise conversion of methanol low excessively cause methyl alcohol can not be in time and hcl reaction just be moved out of reactor drum.Catalyst concn is too high then to cause crystallization easily, and the catalyzer height is main effective residence time of influence reaction also.
Reaction pressure is too high, and material and associated component to reactor drum in industry require will increase investment in fixed assets greatly, and reaction pressure is controlled at 0.01-0.03Mpa (gauge pressure) and is preferred range.
Under the prerequisite that the size of reactor drum 6 is determined, the residence time is the flow decision by the methyl alcohol of putting into reactor drum 6 and hydrogenchloride, according to the flow control residence time of putting into methyl alcohol and hydrogenchloride in the reactor drum 6 be preferable processing condition for 15-40 second.
Main ingredient is monochloro methane and water in the reactor drum 6 outlet components, contains small amount of methanol, hydrogenchloride, by product dme simultaneously.The gaseous component of reactor drum 6 outlet is through condensation, water wash column washing, soda-wash tower alkali cleaning, the washing of sulfuric acid scrubbing tower, again through pressurize and condensation after can to obtain purity be 99.99% high-quality monochloro methane.
The washing of water wash column 8 is to sponge unreacted hydrogenchloride completely for water; Hydrogenchloride is absorbed the back by water and forms 28% hydrochloric acid; The alkali lye neutralisation unit utilizes alkali lye to remove a small amount of hydrogenchloride in the thick monochloro methane, the sulfuric acid drying unit utilize 98% sulfuric acid with the moisture drying in the monochloro methane (gas phase) to 10PPm.
Use present method, conversion of methanol is greater than 99%, and the monochloro methane selectivity is greater than 98.5%, and catalyzer can reach more than 5 years work-ing life.
Reaction mechanism is performed as follows:
CH
3OH+HCl→?CH
3Cl?+H
20 （1）
CH
3OH?+?CH
3OH CH
3O?+?H
20 （2）
Main reaction is (1), and reaction (1) is irreversible strong exothermal reaction, and reaction heat is taken out of through the reactor outlet gaseous component, and reaction (2) is side reaction, can effectively control the generation of byproduct of reaction dme through control catalyst concentration and temperature of reaction.
The present invention utilizes zellon device byproduct hydrogen chloride with the synthetic monochloro methane of industrially scalable; The synthetic monochloro methane can be used for merchandise sales or is used for the raw material of the synthetic methylene dichloride in downstream, trichloromethane, zellon, and techniqueflow provided by the invention is efficiently succinct, and by product is few; Reaction conditions is gentle; Catalyzer is cheap, and has made full use of a large amount of hydrogenchloride of zellon device by-product, helps the chlorine resource and makes full use of.
Description of drawings
Fig. 1 is the process flow diagram that utilizes zellon device byproduct hydrogen chloride to produce monochloro methane of the present invention.
Reference numeral
Embodiment
Below, the present invention is further specified, but the present invention is not limited to said embodiment through exemplary embodiments.
The embodiment of zellon device byproduct hydrogen chloride and the synthetic monochloro methane of methyl alcohol that utilizes of the present invention is following:
Embodiment 1
With zellon device byproduct hydrogen chloride 480Nm
3/ h (170 ℃) condenses to through first condensing surface 1 that 40 ℃, vapour liquid separator 2 separate (flow velocity is 0.3m/s), well heater 3 is heated to 120 ℃, with methyl alcohol 400 Nm from methanol evaporator 4
3/ h (120 ℃) mixes the back through mixing device 5 and introduces reactor drum 6; At liquor zinci chloridi as catalyzer (catalyst concn 50%; The catalyzer addition is reactor drum 6 volumetrical 80%) react under the condition; Maintain is at 130 ℃, and reaction generates monochloro methane under the condition of reaction pressure 0.01 Mpa (gauge pressure), and the hydrogenchloride and the residence time of methyl alcohol in reactor drum 6 of participating in reaction are 40 seconds.Product is about 395Nm
3/ h monochloro methane, reaction mixture are shifted out reactor drum 6 rapidly, and to get purity through 7 condensations of second condensing surface, water wash column 8 washings, the neutralization of soda-wash tower 9 alkali lye, pickling tower 10 sulfuric acid drying, compression, rectifying tower 11 rectifying be 99.99% monochloro methane.
Under the operating mode of this enforcement row 1, conversion of methanol is 99.2%, and the selectivity of monochloro methane is 98.8%.
Zellon device byproduct hydrogen chloride 540Nm
3/ h (170 ℃) condenses to through first condensing surface 1 that 40 ℃, vapour liquid separator 2 separate (flow velocity is 0.1m/s), well heater 3 is heated to 100 ℃, with methyl alcohol 450 Nm from methanol evaporator 4
3/ h (100 ℃) mixes the back through mixing device 5 and introduces reactor drum 6; At liquor zinci chloridi as catalyzer (catalyst concn 80%; The catalyzer addition is reactor drum 6 volumetrical 50%) react under the condition; Maintain is at 110 ℃, and reaction generates monochloro methane under the condition of reaction pressure 0.03Mpa (gauge pressure), and the hydrogenchloride and the residence time of methyl alcohol in reactor drum 6 of participating in reaction are 15 seconds.Product is about 436Nm
3/ h monochloro methane, reaction mixture are shifted out reactor drum 6 rapidly, and to get purity through 7 condensations of second condensing surface, water wash column 8 washings, the neutralization of soda-wash tower 9 alkali lye, pickling tower 10 sulfuric acid drying, compression, rectifying tower 11 rectifying be 99.99% monochloro methane.
Under the operating mode of this enforcement row 2, conversion of methanol MV is 99.3%, and the optionally M.L. of monochloro methane is 98.9%.
Embodiment 3
Zellon device byproduct hydrogen chloride 600Nm
3/ h (170 ℃) condenses to through first condensing surface 1 that 40 ℃, vapour liquid separator 2 separate (flow velocity is 0.24m/s), well heater 3 is heated to 112 ℃, with methyl alcohol 500 Nm from methanol evaporator 4
3/ h (110 ℃) mixes the back through mixing device 5 and introduces reactor drum 6; At liquor zinci chloridi as catalyzer (catalyst concn 70%; The catalyzer addition be reactor volume 68%) react under the condition; Maintain is at 125 ℃, and reaction generates monochloro methane under the condition of reaction pressure 0.02Mpa (gauge pressure), and the hydrogenchloride and the residence time of methyl alcohol in reactor drum of participating in reaction are 32 seconds.Product is about 490Nm
3/ h monochloro methane, reaction mixture are shifted out reactor drum 6 rapidly, and to get purity through 7 condensations of second condensing surface, water wash column 8 washings, the neutralization of soda-wash tower 9 alkali lye, pickling tower 10 sulfuric acid drying, compression, rectifying tower 11 rectifying be 99.99% monochloro methane.
Under the operating mode of this enforcement row, conversion of methanol MV is 99.5%, and the optionally M.L. of monochloro methane is 99.1%.
The above only is preferred embodiment of the present invention, is not to be the restriction of the present invention being made other form, and any professional and technical personnel of being familiar with possibly utilize the technology contents of above-mentioned announcement to change or be modified as the equivalent embodiment of equivalent variations.But everyly do not break away from technical scheme content of the present invention, to any simple modification, equivalent variations and remodeling that above embodiment did, still belong to the protection domain of technical scheme of the present invention according to technical spirit of the present invention.
Claims (5)
1. method of utilizing zellon device byproduct hydrogen chloride to produce monochloro methane comprises:
(a) purification zellon device byproduct hydrogen chloride: will be gasiform raw material zellon device byproduct hydrogen chloride through first condensing surface (1) condensation; Get into then in the vapour liquid separator (2) and separate liquid phase impurity; Get gas phase hydrogenchloride, wherein said first condensing surface (1) temperature out is 40 ℃;
(b) preparation monochloro methane: the said hydrogenchloride that obtains purifying in the step (a) adopts well heater (3) to be heated to 100 ℃-120 ℃; With 100 ℃-120 ℃ methyl alcohol from methanol evaporator (4) is to introduce reactor drum (6) after the mixed of 1.2:1 with the volume ratio through mixing device (5); And be to react the generation monochloro methane under the liquor zinci chloridi condition of 50%-80% in concentration; The addition of said liquor zinci chloridi is said reactor drum (6) volumetrical 50%-80%; Said temperature of reaction is 110 ℃-130 ℃, and gauge pressure is 0.01Mpa-0.03Mpa, and the residence time is 15s-40s;
(c) refining: as the reaction gas phase component of gained in the step (b) promptly to be shifted out said reactor drum (6), more successively through second condensing surface (7) condensation, water wash column (8) washing, the neutralization of soda-wash tower (9) alkali lye, pickling tower (10) sulfuric acid drying, compression, rectifying tower (11).
2. the method for claim 1, the temperature of wherein said raw material zellon device byproduct hydrogen chloride is 170 ℃.
3. the method for claim 1, the purity of the said hydrogenchloride that obtains in the wherein said step (a) is 99.9%.
4. the method for claim 1, wherein the flow velocity of the said gas phase chlorination hydrogen in said vapour liquid separator (2) is 0.1m/s-0.3m/s.
5. the method for claim 1, the length-to-diameter ratio of wherein said vapour liquid separator (2) is 2-4.
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Cited By (11)
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| CN103396286A (en) * | 2013-07-19 | 2013-11-20 | 淮阴师范学院 | Method for producing ethyl chloride by using sodium chloride and low-concentration ethanol as raw materials |
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| CN107308799A (en) * | 2017-06-16 | 2017-11-03 | 浙江金氟隆化工装备有限公司 | A kind of gas purifying device of chlorodifluoromethane |
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| CN103396286A (en) * | 2013-07-19 | 2013-11-20 | 淮阴师范学院 | Method for producing ethyl chloride by using sodium chloride and low-concentration ethanol as raw materials |
| CN103496670A (en) * | 2013-09-12 | 2014-01-08 | 聊城市鲁西化工工程设计有限责任公司 | HCl recovery technique |
| CN103496670B (en) * | 2013-09-12 | 2015-05-13 | 聊城市鲁西化工工程设计有限责任公司 | HCl recovery technique |
| CN103896716A (en) * | 2014-04-16 | 2014-07-02 | 重庆高策科技发展有限公司 | Method for integrated production of tetrachloroethylene, methane chloride and trichlorosilane |
| CN103896716B (en) * | 2014-04-16 | 2015-09-09 | 重庆高策科技发展有限公司 | The method of zellon, methane chloride and trichlorosilane is produced in integration |
| CN104311383A (en) * | 2014-10-15 | 2015-01-28 | 山东东岳氟硅材料有限公司 | Method for producing methane chloride through byproduct hydrogen chloride in production process of tetrachloroethylene |
| CN104311383B (en) * | 2014-10-15 | 2016-05-04 | 山东东岳氟硅材料有限公司 | A kind of method of the hydrogen chloride production monochloro methane that utilizes by-product in tetrachloro-ethylene production process |
| CN107308799A (en) * | 2017-06-16 | 2017-11-03 | 浙江金氟隆化工装备有限公司 | A kind of gas purifying device of chlorodifluoromethane |
| CN108409526A (en) * | 2018-03-09 | 2018-08-17 | 中国化学赛鼎宁波工程有限公司 | A kind of monochloro methane production energy-saving system and method |
| CN108409526B (en) * | 2018-03-09 | 2020-11-20 | 中国化学赛鼎宁波工程有限公司 | Methane chloride energy-saving production system and method |
| CN109081767A (en) * | 2018-09-30 | 2018-12-25 | 南京佳华工程技术有限公司 | A kind of the synthesis rectification technique and its equipment of monochloro methane |
| CN109081767B (en) * | 2018-09-30 | 2021-04-06 | 南京佳华工程技术有限公司 | Synthetic rectification process method and equipment for methane chloride |
| CN111646877A (en) * | 2020-05-25 | 2020-09-11 | 安徽金禾实业股份有限公司 | Method for treating waste hydrochloric acid in sucralose production |
| CN111875471A (en) * | 2020-07-28 | 2020-11-03 | 华陆工程科技有限责任公司 | Methyl chloride synthesis process for cyclic dehydration of catalyst |
| CN111875471B (en) * | 2020-07-28 | 2023-08-29 | 华陆工程科技有限责任公司 | Catalyst circulation dehydration chloromethane synthesis process |
| CN115231986A (en) * | 2022-09-01 | 2022-10-25 | 山东沾化阳光化学有限公司 | Process for producing methane chloride by using hydrogen chloride gas as byproduct of chlorinated ethylene carbonate |
| CN115368205A (en) * | 2022-09-01 | 2022-11-22 | 山东沾化阳光化学有限公司 | Process for producing methane chloride by using hydrogen chloride gas as byproduct of chlorinated paraffin |
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