CN201593028U - Device used in benzyl alcohol continuous hydrolysis technique - Google Patents
Device used in benzyl alcohol continuous hydrolysis technique Download PDFInfo
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- CN201593028U CN201593028U CN2009202531372U CN200920253137U CN201593028U CN 201593028 U CN201593028 U CN 201593028U CN 2009202531372 U CN2009202531372 U CN 2009202531372U CN 200920253137 U CN200920253137 U CN 200920253137U CN 201593028 U CN201593028 U CN 201593028U
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Abstract
The utility model discloses a device used in benzyl alcohol continuous hydrolysis technique, which comprises a first reactor, a second reactor, a third reactor, a forth reactor, a fifth reactor and a sixth reactor. The first reactor is communicated with the second reactor via a first overflow pipe, the second reactor is communicated with the third reactor via a second overflow pipe, the third reactor is communicated with the forth reactor via a third overflow pipe, the forth reactor is communicated with the fifth reactor via a forth overflow pipe, the fifth reactor is communicated with the sixth reactor via a fifth overflow pipe, and the sixth reactor is communicated with a cooling separating tank via a sixth overflow pipe. The device has the advantages that by connecting the six reactors in series, crude benzyl alcohol is eventually obtained by continuous reaction of material inside the six reactors, conversion efficiency is greatly improved with material conversion rate reaching above 99%, and compared with the prior art, the conversion rate can be enhanced more than 65%, thereby sufficiently using the material, lowering production cost and the like.
Description
Technical field
The utility model relates to phenylcarbinol production technique field, specifically is the equipment that a kind of benzyl alcohol continuous hydrolysis technology uses.
Background technology
In phenylcarbinol is produced, take the production of Benzyl Chloride batch hydrolysis mostly at present, be about to react the disposable adding reactor of required sodium carbonate solution after, carry out hydrolysis reaction after slowly adding Benzyl Chloride.The Benzyl Chloride batch hydrolysis requires every batch materials all will experience intensification, temperature-fall period, and this had both prolonged the production cycle, has wasted thermal source again, cause production efficiency low, technology is loaded down with trivial details, reacts insufficient, adopt the Benzyl Chloride batch hydrolysis to produce phenylcarbinol, the reaction completion rate generally only can reach 30%.
Summary of the invention:
The purpose of this utility model is to provide a kind of equipment of benzyl alcohol continuous hydrolysis technology use, it can solve the deficiency that exists in the known technology, utilize 6 cover reactor series connection, mixing liquid in the six cover reactors overflows to next stage step by step by potential difference, mixing liquid constantly reacts in six cover reactors and finally obtains the phenylcarbinol crude product, sufficient reacting, the production efficiency height.
The utility model for achieving the above object, be achieved through the following technical solutions: the equipment that a kind of benzyl alcohol continuous hydrolysis technology uses, comprise first reactor, second reactor, the 3rd reactor, the 4th reactor, the 5th reactor and the 6th reactor, the opening for feed of first reactor is communicated with Benzyl Chloride material source and soda ash solution material source, first reactor is communicated with second reactor by first upflow tube, second reactor is communicated with the 3rd reactor by second upflow tube, the 3rd reactor is communicated with the 4th reactor by the 3rd upflow tube, the 4th reactor is communicated with the 5th reactor by the 4th upflow tube, the 5th reactor is communicated with the 6th reactor by the 5th upflow tube, the 6th reactor is communicated with the cooling separating tank by the 6th upflow tube, the venting port of first reactor is communicated with first condenser, the venting port of second reactor is communicated with second condenser, the venting port of the 3rd reactor is communicated with the 3rd condenser, the venting port of the 4th reactor is communicated with the 4th condenser, the venting port of the 5th reactor is communicated with the 5th condenser, the venting port of the 6th reactor is communicated with the 6th condenser, first condenser, second condenser, the 3rd condenser, the 4th condenser, the liquid outlet of the 5th condenser and the 6th reactor is communicated with first reactor by pipeline respectively, first reactor, second reactor, the 3rd reactor, the 4th reactor, on the 5th reactor and the 6th reactor heating unit is set respectively.
The venting port of described first condenser, second condenser, the 3rd condenser, the 4th condenser, the 5th condenser and the 6th condenser is communicated with carboloy dioxide canister respectively.
In described first reactor, second reactor, the 3rd reactor, the 4th reactor, the 5th reactor and the 6th reactor agitator is installed respectively.
Described heating unit is a heating jacket, and heating jacket is installed on each reactor outer wall, and heating jacket communicates with thermal source and cold water tank respectively by pipeline.
In described second reactor, the 3rd reactor, the 4th reactor, the 5th reactor and the 6th reactor pH value detector is set respectively, second reactor, the 3rd reactor, the 4th reactor, the 5th reactor and the 6th reactor communicate with the sodium carbonate solution source by pipeline respectively, it installs flow control valve respectively on pipeline separately, and the pH value detector in flow control valve and its corresponding reactor is communicated with by lead.
Advantage of the present utility model is: utilize 6 cover reactor series connection, material is constantly reacted in six cover reactors finally obtain the phenylcarbinol crude product, improved transformation efficiency greatly, materials conversion rate can reach more than 99%, relative prior art, transformation efficiency can improve more than 65%, has made full use of material, reduces production costs; Mixing liquid in the six cover reactors overflows to next stage step by step by upflow tube, reduces conveying energy consumption, reduces energy consumption; Be equipped with agitator in the reactor, accelerated reaction changes, and improves transformation efficiency; The carbon dioxide that produces in the equipment can be recovered utilization, reduces atmospheric pollution; Be provided with pH value detector and flowrate control valve, can control the amount of the sodium carbonate solution of carrying automatically in each reactor, need not manual operation, control precisely, and is easy to operate; Simple for structure; The material use is abundant etc.
Description of drawings
Accompanying drawing 1 is a structural representation of the present utility model.
Embodiment
The utility model is described in further detail for the contrast accompanying drawing:
The employed equipment of a kind of benzyl alcohol continuous hydrolysis technology described in the utility model, agent structure has first reactor 11, second reactor 12, the 3rd reactor 13, the 4th reactor 14, the 5th reactor 15 and the 6th reactor 16, the opening for feed of first reactor 11 is communicated with Benzyl Chloride material source and soda ash solution material source, first reactor 11 is communicated with second reactor 12 by first upflow tube 21, second reactor 12 is communicated with the 3rd reactor 13 by second upflow tube 22, the 3rd reactor 13 is communicated with the 4th reactor 14 by the 3rd upflow tube 23, the 4th reactor 14 is communicated with the 5th reactor 15 by the 4th upflow tube 24, the 5th reactor 15 is communicated with the 6th reactor 16 by the 5th upflow tube 25, the 6th reactor 16 is communicated with cooling separating tank 19 by the 6th upflow tube 26, the venting port of first reactor 11 is communicated with first condenser 1, the venting port of second reactor 12 is communicated with second condenser 2, the venting port of the 3rd reactor 13 is communicated with the 3rd condenser 3, the venting port of the 4th reactor 14 is communicated with the 4th condenser 4, the venting port of the 5th reactor 15 is communicated with the 5th condenser 5, the venting port of the 6th reactor 16 is communicated with the 6th condenser 6, first condenser 1, second condenser 2, the 3rd condenser 3, the 4th condenser 4, the liquid outlet of the 5th condenser 5 and the 6th reactor 16 is communicated with first reactor 11 by pipeline respectively, first reactor 11, second reactor 12, the 3rd reactor 13, the 4th reactor 14, on the 5th reactor 15 and the 6th reactor 16 heating unit is set respectively.
In order to reclaim carbonic acid gas, prevent atmospheric pollution, the venting port of first condenser 1, second condenser 2, the 3rd condenser 3, the 4th condenser 4, the 5th condenser 5 and the 6th condenser 6 is communicated with carboloy dioxide canister 10 respectively.
In order to improve the transformation efficiency and the reaction efficiency of first reactor 11, second reactor 12, the 3rd reactor 13, the 4th reactor 14, the 5th reactor 15 and the 6th reactor 16, in first reactor 11, second reactor 12, the 3rd reactor 13, the 4th reactor 14, the 5th reactor 15 and the 6th reactor 16, agitator 8 is installed respectively.
Described heating unit has multiple, preferably adopts heating jacket 7 heating, and heating jacket 7 is installed on each reactor outer wall, and heating jacket 7 communicates with thermal source and cold water tank by pipeline respectively.
Automatic control for pH value in the realization response still, in second reactor 12, the 3rd reactor 13, the 4th reactor 14, the 5th reactor 15 and the 6th reactor 16, pH value detector 18 is set respectively, second reactor 12, the 3rd reactor 13, the 4th reactor 14, the 5th reactor 15 and the 6th reactor 16 communicate with the sodium carbonate solution source by pipeline respectively, it installs flow control valve 17 respectively on pipeline separately, and pH value detector in flow control valve 17 and its corresponding reactor 18 is communicated with by lead.
The technology that the utility model was suitable for is benzyl alcohol continuous hydrolysis technology, comprises following processing step:
(1), add Benzyl Chloride and soda ash solution in first reactor continuously, pressure in first reactor keeps normal pressure, pH value remains on 11-12, temperature of reaction is 95-103 ℃, Benzyl Chloride and soda ash solution react in first reactor, produce the mixing steam and first mixing liquid, comprise water vapour, carbon dioxide and Benzyl Chloride gas in the described mixing steam, mainly comprise phenylcarbinol, Benzyl Chloride and the soda ash solution of generation in described first mixing liquid.Described mixing steam is transported to first condenser by pipeline, and after condensation, the carbon dioxide in the mixing steam is discharged, and the water in the mixing steam and the mixed solution of Benzyl Chloride flow in first reactor by the road, continues to participate in reaction.In first reactor, the transformation efficiency of material reaches 60%-70%.
(2), after the first mixed solution scale of construction in first reactor reaches overflow position, first mixing liquid enters second reactor through first upflow tube, pressure in second reactor keeps normal pressure, pH value remains on 10-11, temperature of reaction is 95-103 ℃, remaining Benzyl Chloride and soda ash solution continues to react in second reactor in first mixing liquid, produce the mixing steam and second mixing liquid, comprise water vapour in the described mixing steam, carbon dioxide and Benzyl Chloride gas mainly comprise the phenylcarbinol of generation in described second mixing liquid, Benzyl Chloride and soda ash solution.Mixing steam is transported to second condenser by pipeline, and after condensation, the carbon dioxide in the mixing steam is discharged, and the water in the mixing steam and the mixed solution of Benzyl Chloride flow in first reactor by the road, continues to participate in reaction.In second reactor, the transformation efficiency of material reaches 75%-80% (alleged transformation efficiency is initial material accumulative total transformation efficiency in first reactor and second reactor, and the following stated transformation efficiency implication is corresponding accumulative total transformation efficiency) herein.
(3), after the second mixed solution scale of construction in second reactor reaches overflow position, second mixing liquid enters the 3rd reactor through second upflow tube, pressure in the 3rd reactor keeps normal pressure, pH value remains on 10-11, temperature of reaction is 95-103 ℃, remaining Benzyl Chloride and soda ash solution continues to react in the 3rd reactor in second mixing liquid, produce mixing steam and the 3rd mixing liquid, comprise water vapour in the described mixing steam, carbon dioxide and Benzyl Chloride gas mainly comprise the phenylcarbinol of generation in described the 3rd mixing liquid, Benzyl Chloride and soda ash solution.Mixing steam is transported to the 3rd condenser by pipeline, and after condensation, the carbon dioxide in the mixing steam is discharged, and the water in the mixing steam and the mixed solution of Benzyl Chloride flow in first reactor by the road, continues to participate in reaction; In the 3rd reactor, the transformation efficiency of material reaches 85%-90%.
(4), after the 3rd mixed solution scale of construction in the 3rd reactor reaches overflow position, the 3rd mixing liquid enters the 4th reactor through the 3rd upflow tube, pressure in the 4th reactor keeps normal pressure, pH value remains on 9-10, temperature of reaction is 95-103 ℃, remaining Benzyl Chloride and soda ash solution continues to react in the 4th reactor in the 3rd mixing liquid, produce mixing steam and the 4th mixing liquid, comprise water vapour in the described mixing steam, carbon dioxide and Benzyl Chloride gas mainly comprise the phenylcarbinol of generation in described the 4th mixing liquid, Benzyl Chloride and soda ash solution.Mixing steam is transported to the 4th condenser by pipeline, and after condensation, the carbon dioxide in the mixing steam is discharged, and the water in the mixing steam and the mixed solution of Benzyl Chloride flow in first reactor by the road, continues to participate in reaction; In the 4th reactor, the transformation efficiency of material reaches 90%-95%.
(6), after the 4th mixed solution scale of construction in the 4th reactor reaches overflow position, the 4th mixing liquid enters the 5th reactor through the 4th upflow tube, pressure in the 5th reactor keeps normal pressure, pH value remains on 9-10, temperature of reaction is 95-103 ℃, remaining Benzyl Chloride and soda ash solution continues to react in the 5th reactor in the 4th mixing liquid, produce mixing steam and the 5th mixing liquid, comprise water vapour in the described mixing steam, carbon dioxide and Benzyl Chloride gas mainly comprise the phenylcarbinol of generation in described the 5th mixing liquid, Benzyl Chloride and soda ash solution.Mixing steam is transported to the 5th condenser by pipeline, and after condensation, the carbon dioxide in the mixing steam is discharged, and the water in the mixing steam and the mixed solution of Benzyl Chloride flow in first reactor by the road, continues to participate in reaction; In the 5th reactor, the transformation efficiency of material reaches more than 95%.
(7), after the 5th mixed solution scale of construction in the 5th reactor reaches overflow position, the 5th mixing liquid enters the 6th reactor through the 5th upflow tube, pressure in the 6th reactor keeps normal pressure, pH value remains on 9-10, temperature of reaction is 95-103 ℃, remaining Benzyl Chloride and soda ash solution continues to react in the 6th reactor in the 5th mixing liquid, produce mixing steam and the 6th mixing liquid, comprise water vapour in the described mixing steam, carbon dioxide and Benzyl Chloride gas mainly are other liquid (less than 1%) of phenylcarbinol (more than 99%) and minute quantity in described the 6th mixing liquid.Mixing steam is transported to the 6th condenser by pipeline, and after condensation, the carbon dioxide in the mixing steam is discharged, and the water in the mixing steam and the mixed solution of Benzyl Chloride flow in first reactor by the road, continues to participate in reaction; In the 6th reactor, the transformation efficiency of material reaches more than 99%.
(8), after the 6th mixed solution scale of construction in the 6th reactor reaches overflow position, the 6th mixing liquid enters the condensation separation jar through the 6th upflow tube, the 6th mixing liquid obtains the phenylcarbinol crude product in the separation of lowering the temperature of condensation separation jar.
In above-mentioned technology, in first reactor, second reactor, the 3rd reactor, the 4th reactor, the 5th reactor and the 6th reactor, be respectively equipped with agitator, agitator stirs the material in the reactor, improves materials conversion rate and reaction efficiency.
The vapor pipe of first condenser, second condenser, the 3rd condenser, the 4th condenser, the 5th condenser and the 6th condenser is communicated with carboloy dioxide canister respectively, isolated carbon dioxide enters the carboloy dioxide canister absorption in the condenser, and the carbonic acid gas of recovery can be used to generate sodium carbonate solution to be used.This programme can reduce emission of carbon-dioxide, reduces environmental pollution.
In this technology, pH value in first reactor need not control because the material abundance can remain in the prescribed value scope.But second reactor, the 3rd reactor, the 4th reactor, the control of the pH value in the 5th reactor and the 6th reactor only relies on its materials inside separately, the low excessively situation of pH value appears sometimes, for this reason at second reactor, the 3rd reactor, the 4th reactor, in the 5th reactor and the 6th reactor pH value control device is set respectively, the pH value control device has a lot, for example manual detection is added sodium carbonate solution etc., the utility model provides a kind of method of automatic control pH value at this, be included in second reactor, the 3rd reactor, the 4th reactor, be respectively equipped with the pH value detector in the 5th reactor and the 6th reactor, second reactor, the 3rd reactor, the 4th reactor, the 5th reactor and the 6th reactor are communicated with the sodium carbonate solution source by pipeline respectively, flow control valve is set respectively on each pipeline, the chain control of flow control valve pH value detector corresponding with it, keep the pH value in each reactor, it is stabilized in the reaction conditions.When pH value in the reactor was low, the pH value detector was controlled its corresponding discharge variable valve automatically, increased the input of sodium carbonate solution; When pH value reached preset requirement in the reactor, the pH value detector was controlled its corresponding discharge variable valve automatically, reduced the input of sodium carbonate solution.
Claims (5)
1. the equipment that uses of a benzyl alcohol continuous hydrolysis technology, it is characterized in that: comprise first reactor (11), second reactor (12), the 3rd reactor (13), the 4th reactor (14), the 5th reactor (15) and the 6th reactor (16), the opening for feed of first reactor (11) is communicated with Benzyl Chloride material source and soda ash solution material source, first reactor (11) is communicated with second reactor (12) by first upflow tube (21), second reactor (12) is communicated with the 3rd reactor (13) by second upflow tube (22), the 3rd reactor (13) is communicated with the 4th reactor (14) by the 3rd upflow tube (23), the 4th reactor (14) is communicated with the 5th reactor (15) by the 4th upflow tube (24), the 5th reactor (15) is communicated with the 6th reactor (16) by the 5th upflow tube (25), the 6th reactor (16) is communicated with cooling separating tank (19) by the 6th upflow tube (26), the venting port of first reactor (11) is communicated with first condenser (1), the venting port of second reactor (12) is communicated with second condenser (2), the venting port of the 3rd reactor (13) is communicated with the 3rd condenser (3), the venting port of the 4th reactor (14) is communicated with the 4th condenser (4), the venting port of the 5th reactor (15) is communicated with the 5th condenser (5), the venting port of the 6th reactor (16) is communicated with the 6th condenser (6), first condenser (1), second condenser (2), the 3rd condenser (3), the 4th condenser (4), the liquid outlet of the 5th condenser (5) and the 6th reactor (16) is communicated with first reactor (11) by pipeline respectively, first reactor (11), second reactor (12), the 3rd reactor (13), the 4th reactor (14), on the 5th reactor (15) and the 6th reactor (16) heating unit is set respectively.
2. the equipment that a kind of benzyl alcohol continuous hydrolysis technology according to claim 1 uses, it is characterized in that: the venting port of first condenser (1), second condenser (2), the 3rd condenser (3), the 4th condenser (4), the 5th condenser (5) and the 6th condenser (6) is communicated with carboloy dioxide canister (10) respectively.
3. the equipment that a kind of benzyl alcohol continuous hydrolysis technology according to claim 5 uses is characterized in that: in first reactor (11), second reactor (12), the 3rd reactor (13), the 4th reactor (14), the 5th reactor (15) and the 6th reactor (16) agitator (8) is installed respectively.
4. the equipment that a kind of benzyl alcohol continuous hydrolysis technology according to claim 3 uses, it is characterized in that: described heating unit is heating jacket (7), heating jacket (7) is installed on each reactor outer wall, and heating jacket (7) communicates with thermal source and cold water tank respectively by pipeline.
5. according to claim 1, the equipment that 3 or 4 each described a kind of benzyl alcohol continuous hydrolysis technologies use, it is characterized in that: second reactor (12), the 3rd reactor (13), the 4th reactor (14), in the 5th reactor (15) and the 6th reactor (16) pH value detector (18) is set respectively, second reactor (12), the 3rd reactor (13), the 4th reactor (14), the 5th reactor (15) and the 6th reactor (16) communicate with the sodium carbonate solution source by pipeline respectively, it installs flow control valve (17) respectively on pipeline separately, and the pH value detector (18) in flow control valve (17) and its corresponding reactor is communicated with by lead.
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| CN2009202531372U CN201593028U (en) | 2009-11-12 | 2009-11-12 | Device used in benzyl alcohol continuous hydrolysis technique |
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| CN2009202531372U CN201593028U (en) | 2009-11-12 | 2009-11-12 | Device used in benzyl alcohol continuous hydrolysis technique |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103121936A (en) * | 2013-01-21 | 2013-05-29 | 安徽雪郎生物科技股份有限公司 | Continuous malic acid synthesizing device and preparation method of malic acid |
| CN101811936B (en) * | 2009-11-12 | 2013-11-06 | 山东聊城中盛蓝瑞化工有限公司 | Benzyl alcohol continuous hydrolysis technology and use equipment thereof |
| CN105315871A (en) * | 2015-11-25 | 2016-02-10 | 华南理工大学 | Device and method for producing super-amphiphobic paint with modification of modified particles |
| CN106187679A (en) * | 2016-06-29 | 2016-12-07 | 山东聊城中盛蓝瑞化工有限公司 | The recycling system and method for carbon dioxide in a kind of chlorinated hydrocabon hydrolysis tail gas |
| CN104926611B (en) * | 2015-05-31 | 2017-05-10 | 湖北绿色家园材料技术股份有限公司 | Novel process for preparing benzyl alcohol by alkali-free continuous hydrolysis of benzyl chloride |
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2009
- 2009-11-12 CN CN2009202531372U patent/CN201593028U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101811936B (en) * | 2009-11-12 | 2013-11-06 | 山东聊城中盛蓝瑞化工有限公司 | Benzyl alcohol continuous hydrolysis technology and use equipment thereof |
| CN103121936A (en) * | 2013-01-21 | 2013-05-29 | 安徽雪郎生物科技股份有限公司 | Continuous malic acid synthesizing device and preparation method of malic acid |
| CN103121936B (en) * | 2013-01-21 | 2015-04-22 | 安徽雪郎生物科技股份有限公司 | Continuous malic acid synthesizing device and preparation method of malic acid |
| CN104926611B (en) * | 2015-05-31 | 2017-05-10 | 湖北绿色家园材料技术股份有限公司 | Novel process for preparing benzyl alcohol by alkali-free continuous hydrolysis of benzyl chloride |
| CN105315871A (en) * | 2015-11-25 | 2016-02-10 | 华南理工大学 | Device and method for producing super-amphiphobic paint with modification of modified particles |
| CN105315871B (en) * | 2015-11-25 | 2017-04-19 | 华南理工大学 | Device and method for producing super-amphiphobic paint with modification of modified particles |
| CN106187679A (en) * | 2016-06-29 | 2016-12-07 | 山东聊城中盛蓝瑞化工有限公司 | The recycling system and method for carbon dioxide in a kind of chlorinated hydrocabon hydrolysis tail gas |
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Granted publication date: 20100929 Termination date: 20121112 |