CN1347862A - Gas and solid phase catalytic process of synthesizing methane chloride - Google Patents
Gas and solid phase catalytic process of synthesizing methane chloride Download PDFInfo
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- CN1347862A CN1347862A CN 01135628 CN01135628A CN1347862A CN 1347862 A CN1347862 A CN 1347862A CN 01135628 CN01135628 CN 01135628 CN 01135628 A CN01135628 A CN 01135628A CN 1347862 A CN1347862 A CN 1347862A
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Abstract
In the presence of efficient active catalyst, methanol and hydrogen chloride in the molar ratio of 1 to 1.02-1.1 and heated to over 200 deg.c are made to react in a reactor at 240-300 deg.c temperature and 0-0.5 MPa pressure for 4-6 sec to form the mixture of methane chloride and unreacted anhydrous hydrogen chloride. The mixture is further produced into methane chloride through water washing, alkali pickling and sulfuric acid drying. The process of the present invention has a methanol converting rate over 98 %, methane chloride selectivity over 98 % and catalyst life of 7500-8400 hr. In addition, circular water absorption in adopted and this can safev water and reduce environmental pollution.
Description
Technical field
The present invention relates to gas and solid phase catalytic process of synthesizing methane chloride.
Background technology
The method that generally adopts of monochloro methane suitability for industrialized production has two kinds in the world: namely for methane chlorination and methyl alcohol hydrochlorinate method. along with the construction of methyl alcohol large chemical plant and be subjected to the influence of hydrogenchloride market, from the eighties not methyl alcohol method route occupy an leading position, this method has the single advantage of product.
The methyl alcohol chlorination reaction can be carried out in liquid phase or gas phase.Catalyzer is the aqueous solution of metal chlorides such as iron trichloride or zinc chloride, reactor is generally the Steel Vessel of liner enamel or acid resisting brick, bubbling feeds equimolar methyl alcohol and the reaction of chlorination chlorine body generates monochloro methane and water, temperature is controlled at 110～180 ℃, prevents to be taken away the variation that causes catalyst concn by reactant gases because of the condensation of water generation reaction or the moisture of catalyzer.The water that generates in the reaction also has unconverted methyl alcohol and chlorination chlorine and dimethyl ether as byproduct in addition along with the steam of methyl chloride is taken out of together, and thick product obtains product at last through technological processs such as washing, alkali cleaning, dryings.Liquid phase reaction is to carry out in the reactor of catalyst solution is housed, and the throughput of reactor is owing to the influence of bubbling speed is restricted.
Solid catalyst is mainly adopted in gas solid method production, generally after being preheating to 180～200 ℃ after the mixed in molar ratio such as methanol steam and hydrogenchloride, enter reactor, has reactor throughput advantage of higher, but because exothermic heat of reaction, temperature is controlled easily not as liquid phase method, and the dme amount of generation is also higher, and reaction must be carried out under comparatively high temps, conversion of methanol is 92～96%, and the yield of monochloro methane is about 95%.
Solid catalyst comprises zinc chloride, cupric chloride and phosphoric acid isoreactivity composition, and they are deposited on gac, silica gel, float stone and the aluminum oxide usually, also can directly use aluminum oxide as catalyzer.
In the production technique of above-mentioned multiple monochloro methane, gas solid method has advantages such as throughput is big, range of product is single, easily separated, but if no a kind of efficient, active catalyst, then Fan Ying transformation efficiency is low, both influence unit consumption of product, increased the burden of back system again.Adopt traditional catalyzer, as aluminum oxide etc., activity is low when low temperature, and during high temperature the life-span short, resulting reactivity worth (conversion, selectivity, life-span) is uneconomic.
Summary of the invention
Of the present inventionly provide a kind of gas and solid phase catalytic process of synthesizing methane chloride.
It is 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 ℃ enter the reactor internal reaction, temperature of reaction is 240 ℃～300 ℃, 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.
The present invention can make the synthetic methanol conversion of producing of gas and solid phase catalytic 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.Adopted the water-washing method different, changed direct current water spray absorption technique, like this, both can improve the assimilated efficiency of tower, saved the add-on of fresh water, can improve the hydrochloric acid of waste strength to 25% again, turned waste into wealth, reduced environmental pollution for circulation absorbs with routine.Water and dme remove the traditional sulfuric acid drying process of main employing.Dried purity is extremely stored below-20 ℃ greater than 99.9% monochloro methane condensation of gas.
Description of drawings
Fig. 1 is a kind of gas and solid phase catalytic process of synthesizing methane chloride schema;
Fig. 2 is another kind of gas and solid phase catalytic process of synthesizing methane chloride schema.
Embodiment
The present invention is that the catalyzer of main ingredient can be a cylindrical shape with the gama-alumina with what produce, also can be other shape that other has identical specific surface area, intensity and porosity.Reach a little Preparation of catalysts and typing and at first will carry out the dissolving of metal-salt, coprecipitated, the operation of then wash again, the technician in Catalyst Production fields such as filtration, spraying drying, calcination, pre-compressing tablet, fragmentation, compression molding grasping with alkali.The component of high-efficiency activated catalyzer is 1 part of gama-alumina, 0.8～1.5 part of Na
2O, 0.2～0.3 part of SO
3, 0.01～0.02 part of Fe
2O
3, 0.4～0.5 part of SiO
2The specification of catalyzer is: cylindrical Φ 3-5mm
*H5mm, tap density: 0.78～0.88kg/L, ultimate compression strength:＞400Kg/cm
3, specific surface area: 160～270m
2/ g, porosity: about 40～60%, SiO
2: be lower than 0.5% (wt), SO
3: be lower than 0.3% (wt), Fe
2O
3: be lower than 0.02% (wt), Na
2O:0.8～1.4% (wt), ignition loss: be lower than 3.4% (wt) (reference value) (600 ℃/1hr), H
2O: be lower than 0.91% (wt), wherein Na
2The content outbalance of O, it directly has influence on activity of such catalysts.Temperature of reaction is also very important, this reaction is thermo-negative reaction, temperature raises, can accelerate reaction process, improve conversion of raw material, but temperature is when being higher than 300 ℃, activity of such catalysts can descend greatly, life-span quicken to shorten, and when temperature of reaction is lower than 250 ℃, and conversion of methanol decreases and the content of dimethyl ether as byproduct can increase.
The used catalyzer of the present invention is based on aluminum oxide, and is coprecipitated through dissolving and alkali, washs, filters, and adds trace element, spraying drying, calcination, pre-compressing tablet, fragmentation, several operation in the compression molding or all operation and the effective catalyst for preparing.
Of the present invention be in the presence of the catalyzer of main ingredient with the gama-alumina, hydrogenchloride and methanol gas are reacted, for guaranteeing that methyl alcohol has higher transformation efficiency, make hydrogenchloride excessive slightly, the mol ratio of hydrogenchloride and methyl alcohol is about 1.02～1.1: 1, and two kinds of gases are heated to respectively more than 200 ℃ when entering reactor, and reactor temperature is controlled at 240～300 ℃, pressure 0～0.5MpaG, residence time of material 4～6 seconds answers temperature to regulate by the flow of the outer thermal oil of reactor.Reactor adopts fixed-bed reactor, and material adopts corrosion resistant material, and for preventing expanding with heat and contract with cold of material, tubulation adopts particular form to fix in the reactor.
From the air-flow that reactor comes out, contain CH
3CL, HCL, CH
3OH, (CH
3)
2O, H
2O etc. for obtaining purity greater than the product more than 99.9%, need carry out a series of refining.In order to remove the excessive hydrogenchloride in the mixed gas, can take washing and alkali cleaning.Here, we have adopted the water-washing method different with routine, change direct current water spray absorption technique and absorb for circulation.
Gas and solid phase catalytic process of synthesizing methane chloride is in the presence of high-efficiency activated catalyzer, mol ratio is 1: 1.02, the methyl alcohol and the hydrogenchloride that are heated to more than 200 ℃ enter the reactor internal reaction, temperature of reaction is 240 ℃, reaction pressure is 0MpaG, reaction times is 4 seconds, and the monochloro methane of generation and unconverted anhydrous hydrogen chloride make monochloro methane through washing, alkali cleaning and sulfuric acid drying.
Gas and solid phase catalytic process of synthesizing methane chloride is to be in the presence of high-efficiency activated catalyzer, mol ratio is 1: 1.1, the methyl alcohol and the hydrogenchloride that are heated to more than 200 ℃ enter the reactor internal reaction, temperature of reaction is 300 ℃, reaction pressure is 0.5MpaG, reaction times is 6 seconds, and the monochloro methane of generation and unconverted anhydrous hydrogen chloride make monochloro methane through washing, alkali cleaning and sulfuric acid drying.
Flow process by manufacturing shown in Figure 1 is produced monochloro methane.The methyl alcohol that uses is the high purity refined methanol, and water content is lower than 0.1%, and ethanol content is lower than 0.03%, and chlorination chlorine is that purity is greater than 99.9% anhydrous hydrogen chloride.Methyl alcohol and hydrogenchloride are the gas more than 200 ℃.
The feed rate of material benzenemethanol: 450NM
3/ H
The feed rate of hydrogenchloride is 495NM
3/ H
Temperature of reactor: 250～300 ℃
Reactor pressure: 0.1～0.3MpaG
Water wash column process water inlet amount 0.2M
3/ H
The output of monochloro methane (normal temperature) is 1.058M
3/ H
Record by above-mentioned experiment, conversion of methanol is 98%, and the yield of monochloro methane after washing, alkali cleaning is 96%.
Flow process by manufacturing shown in Figure 2 is produced monochloro methane.The methyl alcohol that uses is the high purity refined methanol, and water content is lower than 0.1%, and ethanol content is lower than 0.03%, and chlorination chlorine is that purity is greater than 99.9% anhydrous hydrogen chloride.Methyl alcohol and hydrogenchloride are the gas phase more than 200 ℃.
The feed rate of material benzenemethanol: 450NM
3/ H
The feed rate of hydrogenchloride is 495NM3/H
Temperature of reactor: 250～300 ℃
Reactor pressure: 0.1～0.3MpaG
Water wash column process water inlet amount 1M
3/ H
The output of monochloro methane (normal temperature) is 1.05M
3/ H
By above-mentioned test, conversion of methanol is 98%, and the yield of monochloro methane after washing, alkali cleaning is 95.2%.
Claims (4)
1. gas and solid phase catalytic process of synthesizing methane chloride, it is characterized in that 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 ℃ enter the reactor internal reaction, temperature of reaction is 240 ℃～300 ℃, reaction pressure is 0～0.5MpaG, and the 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.
2. a kind of gas and solid phase catalytic process of synthesizing methane chloride according to claim 1, the component that it is characterized in that said high-efficiency activated catalyzer are 1 part of gama-alumina, 0.8～1.5 part of Na
2O, 0.2～0.3 part of SO
3, 0.01～0.02 part of Fe
2O
3, 0.4～0.5 part of SiO
2
3. a kind of gas and solid phase catalytic process of synthesizing methane chloride according to claim 1 is characterized in that said reactor adopts fixed-bed reactor, and material adopts corrosion resistant material.
4. a kind of gas and solid phase catalytic process of synthesizing methane chloride according to claim 1 is characterized in that said washing employing circulation absorption process.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011356286A CN1164543C (en) | 2001-10-08 | 2001-10-08 | Gas and solid phase catalytic process of synthesizing methane chloride |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011356286A CN1164543C (en) | 2001-10-08 | 2001-10-08 | Gas and solid phase catalytic process of synthesizing methane chloride |
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|---|---|
| CN1347862A true CN1347862A (en) | 2002-05-08 |
| CN1164543C CN1164543C (en) | 2004-09-01 |
Family
ID=4673219
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|---|---|---|---|
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100432033C (en) * | 2004-07-16 | 2008-11-12 | 株式会社德山 | Method for producing methyl chloride and method for producing highly chlorinated methanes |
| CN102234215A (en) * | 2010-04-23 | 2011-11-09 | 天津市泰亨气体有限公司 | Technology for producing methyl chloride by gas-solid phase catalytic method |
| CN101429093B (en) * | 2008-11-28 | 2011-11-09 | 北京石油化工设计院有限公司 | Energy-saving process for producing monochloro methane with liquid phase catalysis method |
| CN101559313B (en) * | 2008-04-18 | 2012-08-08 | 上海汇友精密化学品有限公司 | Method for reducing sewage discharge in washed method |
| CN103193251A (en) * | 2013-03-26 | 2013-07-10 | 北京烨晶科技有限公司 | Technology for jointly producing ammonium sulfate and chloromethane |
| CN103567170A (en) * | 2012-07-31 | 2014-02-12 | 曹汉平 | Method for removing scaling substances of methane chloride of chlorinating device |
| CN104645883A (en) * | 2015-02-12 | 2015-05-27 | 东至绿洲环保化工有限公司 | Organic silicon production device |
| CN105728062A (en) * | 2014-12-11 | 2016-07-06 | 中国石油化工股份有限公司 | Production method for copper-zinc catalyst |
| CN105727960A (en) * | 2014-12-11 | 2016-07-06 | 中国石油化工股份有限公司 | A preparing method of a methanol synthesis catalyst used for a slurry bed |
| CN107490315A (en) * | 2017-09-18 | 2017-12-19 | 南通华耐特石墨设备有限公司 | A kind of energy-saving graphite heat exchanger and production method that heat energy is synthesized using monochloro methane |
| CN107715902A (en) * | 2017-09-05 | 2018-02-23 | 丁章云 | A kind of gas-solid phase chloromethanes catalyst and its preparation method |
-
2001
- 2001-10-08 CN CNB011356286A patent/CN1164543C/en not_active Expired - Lifetime
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100432033C (en) * | 2004-07-16 | 2008-11-12 | 株式会社德山 | Method for producing methyl chloride and method for producing highly chlorinated methanes |
| CN101559313B (en) * | 2008-04-18 | 2012-08-08 | 上海汇友精密化学品有限公司 | Method for reducing sewage discharge in washed method |
| CN101429093B (en) * | 2008-11-28 | 2011-11-09 | 北京石油化工设计院有限公司 | Energy-saving process for producing monochloro methane with liquid phase catalysis method |
| CN102234215A (en) * | 2010-04-23 | 2011-11-09 | 天津市泰亨气体有限公司 | Technology for producing methyl chloride by gas-solid phase catalytic method |
| CN103567170A (en) * | 2012-07-31 | 2014-02-12 | 曹汉平 | Method for removing scaling substances of methane chloride of chlorinating device |
| CN103193251A (en) * | 2013-03-26 | 2013-07-10 | 北京烨晶科技有限公司 | Technology for jointly producing ammonium sulfate and chloromethane |
| CN103193251B (en) * | 2013-03-26 | 2014-12-10 | 北京烨晶科技有限公司 | Technology for jointly producing ammonium sulfate and chloromethane |
| CN105728062A (en) * | 2014-12-11 | 2016-07-06 | 中国石油化工股份有限公司 | Production method for copper-zinc catalyst |
| CN105727960A (en) * | 2014-12-11 | 2016-07-06 | 中国石油化工股份有限公司 | A preparing method of a methanol synthesis catalyst used for a slurry bed |
| CN104645883A (en) * | 2015-02-12 | 2015-05-27 | 东至绿洲环保化工有限公司 | Organic silicon production device |
| CN107715902A (en) * | 2017-09-05 | 2018-02-23 | 丁章云 | A kind of gas-solid phase chloromethanes catalyst and its preparation method |
| CN107490315A (en) * | 2017-09-18 | 2017-12-19 | 南通华耐特石墨设备有限公司 | A kind of energy-saving graphite heat exchanger and production method that heat energy is synthesized using monochloro methane |
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|---|---|
| CN1164543C (en) | 2004-09-01 |
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Granted publication date: 20040901 |