CN209906674U - Device for continuously producing dichloropinacolone by differential circulation - Google Patents
Device for continuously producing dichloropinacolone by differential circulation Download PDFInfo
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- CN209906674U CN209906674U CN201920452623.0U CN201920452623U CN209906674U CN 209906674 U CN209906674 U CN 209906674U CN 201920452623 U CN201920452623 U CN 201920452623U CN 209906674 U CN209906674 U CN 209906674U
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Abstract
The utility model provides a device for continuously producing dichloropinacolone by differential circulation, which comprises a main reactor, a pre-reactor, a separator, a circulating pump, a discharging pump, a pipeline and a self-control instrument, the main reactor and the prereactor are tubular microchannel reaction heat exchanger, all have a plurality of fore-and-aft tube side and a plurality of horizontal shell side, and the shell side is used for the cooling, and the tube side is used for carrying the material, the utility model discloses a differential circulation technique has reduced the production of trichloro pinacolone, has improved the yield of product, utilizes the prereactor to take place chemical reaction and desorption with the pinacolone of newly-added in with tail gas hydrogen chloride gas free chlorine, saves the side reaction problem of sodium hypochlorite that brings with the method of alkali wash, and the chlorination liquid after the reaction adopts the vacuum dehydrochlorination technique to realize the high-efficient separation of dichloro pinacolone and the hydrogen chloride of dissolving in the chlorination liquid, replaces the environmental protection problem that the dechlorination of adding water of traditional intermittent type method brought waste hydrochloric acid production.
Description
Technical Field
The utility model relates to a fine chemical industry field, concretely relates to device of differential circulation continuous production dichloro pinacolone.
Background
Dichloro pinacolone is an important raw material and intermediate for organic synthesis. Can be widely used as pesticide and medical intermediate, and is also used for preparing triazolone fungicide in the past.
The dichloro-pinacolone is synthesized by chlorination of pinacolone with chlorine.
The process principle is as follows:
adding metered chloropinacolone into a chlorination reaction kettle, heating the chlorine to 40 ℃, introducing the chlorine into the chlorination reaction kettle through a buffer tank, and carrying out heat preservation reaction for 70 hours at the temperature. And simultaneously, starting a tail gas absorption device, absorbing associated hydrogen chloride into hydrochloric acid through water, and absorbing excessive chlorine through liquid caustic soda to generate a waste liquid containing sodium hypochlorite for centralized treatment. After the reaction is finished, adding water into the kettle for cooling, and washing until the solution does not contain chloride ions. Filtering to obtain waste liquid, cooling and packaging crystal to obtain product
The production method is an intermittent production process, is simple and convenient, is flexible to operate, and has the disadvantages of high raw material consumption, long production period, large equipment investment (more reaction kettles), high cost and serious pollution.
At present, under the new requirements of energy efficiency multiplication and economic sustainable development, a novel energy-saving, consumption-reducing and environment-friendly dichloropinacolone production method is needed.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a differential circulation continuous production dichloro pinacolone's device to solve the problem that proposes among the above-mentioned background art.
In order to achieve the above object, the utility model provides a following technical scheme:
a device for producing pinacolone by a continuous method comprises a main reactor, a pre-reactor, a separator, a circulating pump, a discharge pump, a demister, a pipeline and a self-control instrument, wherein the main reactor is a tubular micro-channel reaction heat exchanger, it has a plurality of longitudinal main reactor tube sides and a plurality of transverse main reactor shell sides, two ends of the main reactor shell sides are respectively connected with a main reactor cooling water inlet and a main reactor cooling water outlet which are arranged at two sides of the main reactor, the bottom of the main reactor is provided with a gas-liquid mixing chamber, the bottom of the gas-liquid mixing chamber is provided with a gas inlet of the main reactor, the side surface of the gas-liquid mixing chamber is provided with a liquid inlet of the main reactor, the gas-liquid mixing chamber is internally provided with a high-efficiency mixing structure body, the middle part of the main reactor is provided with a gas distributor, the gas distributor is provided with a chlorine inlet of the main reactor, the upper end and the lower end of the tube pass of the main reactor are respectively connected with a main reactor discharge hole and a gas-liquid mixing chamber at the top of the main reactor;
the pre-reactor is a tubular micro-channel reaction heat exchanger and is provided with a plurality of longitudinal pre-reactor tube passes and a plurality of transverse pre-reactor shell passes, the upper end in the pre-reactor is provided with a filler tower section, the two ends of the pre-reactor shell passes are respectively connected with a pre-reactor cooling water inlet and a pre-reactor cooling water outlet which are arranged at the two sides of the pre-reactor, the bottom of the pre-reactor is provided with a pre-reactor mixing chamber, the bottom of the pre-reactor mixing chamber is provided with a pre-reactor mixed liquid outlet, the side surface of the pre-reactor is provided with a pre-reactor gas inlet, the top of the pre-reactor is provided with a pre-reactor separation chamber, the side surface of the pre-;
the top of the separator is provided with a separator feeding port and a separator air outlet, and the bottom of the separator is provided with a separator chlorine inlet and a separator discharge port;
gaseous entry of main reactor and the gaseous entry of main reactor let in chlorine, and the separator pan feeding mouth is connected to the main reactor discharge gate, the gaseous entry linkage separator gas outlet of pre-reactor, the entry of defroster is connected to the discharge gate of pre-reactor, and the export liquid phase of defroster is connected and the circulating pump entry, and hydrogen chloride absorption equipment is connected to the gaseous phase, and the exit linkage main reactor liquid entry of circulating pump, separator chlorine import let in chlorine, and the entry of circulating pump and the entry of ejection of compact pump are connected to the separator discharge gate, the exit linkage splitter of ejection of compact pump.
Preferably, the main reactor tube side and the pre-reactor tube side are both filled with micro-channel ceramic fillers, the diameter of each micro-channel ceramic filler is 8-100 mm, the diameter of the main reactor tube side is 10-110 mm, and the diameter of the pre-reactor tube side is 8-120 mm.
Preferably, the diameter of the micro-channel ceramic filler is 14-64 mm, the diameter of the main reactor tube side is 15-65 mm, and the diameter of the pre-reactor tube side is 30-100 mm.
Preferably, the main bodies of the main reactor and the pre-reactor are made of one or more of titanium alloy, impregnated graphite, carbon steel and silicon carbide, and the shells of the main reactor and the pre-reactor are made of carbon steel.
Preferably, the top of the separator is provided with a separator return port, and the separator return port is connected with the pre-reactor mixed liquid outlet.
Compared with the prior art, the utility model has the advantages of it is following:
(1) equipment investment is saved:
because the generation of trichloro-pinacolone in the chlorination liquid is reduced and the reaction selectivity is improved by a differential circulation technology (the chlorination liquid and the chlorine are fully contacted in a microchannel of a main reactor by a circulating pump, the retention time is increased, the temperature of the reaction process is controlled, and the chlorine and the chlorination liquid in the chlorination liquid are introduced in three places to avoid deep chlorination, which is called as differential circulation reaction), compared with the traditional technology, one set of device can replace dozens of reaction kettles, and the whole equipment investment is reduced;
(2) the production efficiency is high:
the whole body forms circulation continuous production, and a micro-channel mechanism is adopted in a main reactor and a pre-reactor, so that the reaction efficiency is greatly improved, chlorine gas reacts with chlorination liquid through three places, the generation of side reaction trichloropinacolone is effectively avoided, and the product quality of the dichloropinacolone is improved;
(3) green and environment-friendly:
the chlorine solution is subjected to removal of dissolved hydrogen chloride gas by a rotary film evaporator in a vacuum state, so that pollution of waste hydrochloric acid caused by washing the hydrogen chloride by adding water in an intermittent method can be avoided; the hydrogen chloride generated by the tail gas can intercept more than 98% of 1um liquid through a demister, and the high-purity hydrogen chloride can be used for producing downstream hydrochlorination products. Compared with the prior art, the whole production process has no three wastes, is a self-cleaning process and achieves the aim of circular economy.
Drawings
FIG. 1 is a flow chart of the overall structure of the present invention;
FIG. 2 is a schematic structural view of a main reactor of the present invention;
FIG. 3 is a schematic diagram of a pre-reactor of the present invention;
fig. 4 is a schematic structural diagram of the separator of the present invention.
In the figure: 1-main reactor, 2-pre-reactor, 3-separator, 101-gas distributor, 102-main reactor shell side, 103-main reactor cooling water outlet, 104-main reactor discharge outlet, 105-main reactor tube side, 106-main reactor cooling water inlet, 107-main reactor chlorine inlet, 108-gas-liquid mixing chamber, 109-high efficiency mixing structure, 110-main reactor gas inlet, 111-main reactor liquid inlet, 201-pre-reactor shell side, 202-pinacolone feed inlet, 203-pre-reactor discharge outlet, 204-pre-reactor separation chamber, 205-pre-reactor cooling water outlet, 206-pre-reactor tube side, 207-packed tower section, 208-pre-reactor mixing chamber, 209-reactor gas inlet, 210-a mixed liquid outlet of the pre-reactor, 211-a cooling water inlet of the pre-reactor, 301-a gas outlet of the separator, 302-a discharge hole of the separator, 303-a material inlet of the separator, 304-a reflux hole of the separator and 305-a chlorine inlet of the separator.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Referring to fig. 1-4, a device for differential circulation continuous production of dichloropinacolone comprises a main reactor 1, a pre-reactor 2, a separator 3, a circulating pump, a discharge pump, a demister, a pipeline and a self-control instrument, wherein the main reactor 1 is a tubular microchannel reaction heat exchanger, and is provided with a plurality of longitudinal main reactor tube passes 105 and a plurality of transverse main reactor shell passes 102, two ends of the main reactor shell passes 102 are respectively connected with a main reactor cooling water inlet 106 and a main reactor cooling water outlet 103 which are arranged at two sides of the main reactor 1, a gas-liquid mixing chamber 108 is arranged at the bottom of the main reactor 1, a main reactor gas inlet 110 is arranged at the bottom of the gas-liquid mixing chamber 108, a main reactor liquid inlet 111 is arranged at the side, a high-efficiency mixing structure body 109 is arranged in the gas-liquid mixing chamber 108, a gas distributor 101 is arranged at the middle part of the main, a chlorine inlet 107 of the main reactor is arranged on the gas distributor 101, and the upper end and the lower end of the tube pass 105 of the main reactor are respectively connected with a main reactor discharge hole 104 and a gas-liquid mixing chamber 108 at the top of the main reactor 1;
the pre-reactor 2 is a tubular micro-channel reaction heat exchanger and is provided with a plurality of longitudinal pre-reactor tube passes 206 and a plurality of transverse pre-reactor shell passes 201, the upper end of the pre-reactor 2 is provided with a filler tower section 207, two ends of the pre-reactor shell passes 201 are respectively connected with a pre-reactor cooling water inlet 211 and a pre-reactor cooling water outlet 205 which are arranged at two sides of the pre-reactor 2, the bottom of the pre-reactor 2 is provided with a pre-reactor mixing chamber 208, the bottom of the pre-reactor mixing chamber 208 is provided with a pre-reactor mixed liquid outlet 210, the side surface is provided with a pre-reactor gas inlet 209, the top of the pre-reactor 2 is provided with a pre-reactor separation chamber 204, the side surface of the pre-reactor separation chamber 204 is provided with a;
the top of the separator 3 is provided with a separator feeding port 303 and a separator gas outlet 301, and the bottom of the separator 3 is provided with a separator chlorine inlet 305 and a separator discharge port 302;
the chlorine is introduced into a main reactor gas inlet 110 and a main reactor chlorine inlet 107, a main reactor discharge port 104 is connected with a separator feeding port 303, a pre-reactor gas inlet 209 is connected with a separator gas outlet 301, a pre-reactor discharge port 203 is connected with an inlet of a demister, an outlet liquid phase of the demister is connected with an inlet of a circulating pump, a gas phase is connected with a hydrogen chloride absorption device, an outlet of the circulating pump is connected with a main reactor liquid inlet 111, a chlorine inlet 305 of the separator is introduced into the chlorine, a separator discharge port 302 is connected with an inlet of the circulating pump and an inlet of a discharge pump, and an outlet of the discharge pump.
The main reactor tube side 105 and the pre-reactor tube side 206 are both filled with micro-channel ceramic fillers, the diameter of each micro-channel ceramic filler is 8-100 mm, the diameter of the main reactor tube side 105 is 10-110 mm, and the diameter of the pre-reactor tube side 206 is 8-120 mm.
Preferably, the diameter of the micro-channel ceramic filler is 14-64 mm, the diameter of the main reactor tube side 105 is 15-65 mm, and the diameter of the pre-reactor tube side 206 is 30-100 mm.
The main bodies of the main reactor 1 and the pre-reactor 2 are made of one or more of titanium alloy, impregnated graphite, carbon steel and silicon carbide, and the shells of the main reactor 1 and the pre-reactor 2 are made of carbon steel.
Wherein, the top of the separator 3 is provided with a separator return port 304, and the separator return port 304 is connected with the pre-reactor mixed liquid outlet 210.
The first embodiment is as follows:
step 1: the chloridized liquid in the separator 3 and chlorine introduced from a chlorine inlet 305 of the separator are subjected to chemical reaction, the chloridized liquid is discharged from a discharge hole 302 of the separator, is pressurized by a circulating pump, enters a gas-liquid mixing chamber 108 from a liquid inlet 111 of a main reactor, is fully mixed with chlorine introduced from a gas inlet 110 of the main reactor under the action of a high-efficiency mixing structure 109, the mixed liquid enters a tube pass 105 of the main reactor for chemical reaction, one path of chlorine enters from a chlorine inlet 107 of the main reactor, is uniformly dispersed by a gas distributor 101, is subjected to chemical reaction (the reaction temperature is 35 ℃ and the reaction pressure is 80KPa) with the mixed liquid in the tube pass 105 of the main reactor, and is cooled by cooling water in a shell pass through a discharge hole 104 of the main reactor and a feed hole 303 of the separator, and flows back to the separator 3 for gas-;
step 2: the separated hydrogen chloride gas is discharged from a gas outlet 301 of the separator and then enters a pre-reactor mixing chamber 208 through a pre-reactor gas inlet 209, and the chloride solution in the separator 3 enters the main reactor 1 again through the circulating pump to continue to react;
when the concentration of the dichloropinacolone in the chlorination liquid in the separator 3 reaches more than 97 percent, the chlorination liquid is pumped out through a discharge pump and sent to dehydrochlorination equipment, hydrogen chloride gas dissolved in the chlorination liquid is removed under vacuum, the solution is cooled and crystallized into the dichloropinacolone, and the hydrogen chloride is absorbed into hydrochloric acid by water;
and step 3: free chlorine carried by hydrogen chloride gas reacts in the pre-reactor 2 (the reaction temperature is 20 ℃, the reaction pressure is 80KPa) and rises to a pre-reactor separation chamber 204, the free chlorine is mixed with pinacolone added from a pinacolone feed port 202, the carried liquid is recovered, the hydrogen chloride gas is discharged from a pre-reactor discharge port 203 and enters a demister, and the hydrogen chloride gas is cooled by cooling water in a pre-reactor shell side 201 during the reaction of the pre-reactor 2;
and 4, step 4: the demister traps hydrogen chloride liquid drops carried in the hydrogen chloride gas, and the hydrogen chloride gas enters hydrogen chloride absorption equipment;
and 5: the hydrogen chloride liquid drops separated in the demister and the mixed liquid discharged from the discharge port 302 of the separator are converged and then pumped into the main reactor 1 through a circulating pump.
Example two:
step 1: the chloridized liquid in the separator 3 and chlorine introduced from a chlorine inlet 305 of the separator are subjected to chemical reaction, the chloridized liquid is discharged from a discharge hole 302 of the separator, is pressurized by a circulating pump, enters a gas-liquid mixing chamber 108 from a liquid inlet 111 of a main reactor, is fully mixed with chlorine introduced from a gas inlet 110 of the main reactor under the action of a high-efficiency mixing structure 109, the mixed liquid enters a tube pass 105 of the main reactor for chemical reaction, one path of chlorine enters from a chlorine inlet 107 of the main reactor, is uniformly dispersed by a gas distributor 101, is subjected to chemical reaction (the reaction temperature is 75 ℃ and the reaction pressure is 250KPa) with the mixed liquid in the tube pass 105 of the main reactor, and is cooled by cooling water in a shell pass through a discharge hole 104 of the main reactor and a feed hole 303 of the separator, and flows back to the separator 3 for gas-;
step 2: the separated hydrogen chloride gas is discharged from a gas outlet 301 of the separator and then enters a pre-reactor mixing chamber 208 through a pre-reactor gas inlet 209, and the chloride solution in the separator 3 enters the main reactor 1 again through the circulating pump to continue to react;
when the concentration of the dichloropinacolone in the chlorination liquid in the separator 3 reaches more than 97 percent, the chlorination liquid is pumped out through a discharge pump and sent to dehydrochlorination equipment, hydrogen chloride gas dissolved in the chlorination liquid is removed under vacuum, the solution is cooled and crystallized into the dichloropinacolone, and the hydrogen chloride is absorbed into hydrochloric acid by water;
and step 3: free chlorine carried by hydrogen chloride gas reacts in the pre-reactor 2 (the reaction temperature is 65 ℃, the reaction pressure is 250KPa) and rises to a pre-reactor separation chamber 204, the free chlorine is mixed with pinacolone added from a pinacolone feed inlet 202, the carried liquid is recovered, the hydrogen chloride gas is discharged from a pre-reactor discharge port 203 and enters a demister, and the hydrogen chloride gas is cooled by cooling water in a pre-reactor shell side 201 during the reaction of the pre-reactor 2;
and 4, step 4: the demister traps hydrogen chloride liquid drops carried in the hydrogen chloride gas, and the hydrogen chloride gas enters hydrogen chloride absorption equipment;
and 5: the hydrogen chloride liquid drops separated in the demister and the mixed liquid discharged from the discharge port 302 of the separator are converged and then pumped into the main reactor 1 through a circulating pump.
Example three:
step 1: the chloridized liquid in the separator 3 and chlorine introduced from a chlorine inlet 305 of the separator are subjected to chemical reaction, the chloridized liquid is discharged from a discharge hole 302 of the separator, is pressurized by a circulating pump, enters a gas-liquid mixing chamber 108 from a liquid inlet 111 of a main reactor, is fully mixed with chlorine introduced from a gas inlet 110 of the main reactor under the action of a high-efficiency mixing structure 109, the mixed liquid enters a tube pass 105 of the main reactor for chemical reaction, one path of chlorine enters from a chlorine inlet 107 of the main reactor, is uniformly dispersed by a gas distributor 101, is subjected to chemical reaction (the reaction temperature is 55 ℃ and the reaction pressure is 165KPa) with the mixed liquid in the tube pass 105 of the main reactor, and is cooled by cooling water in a shell pass through a discharge hole 104 of the main reactor and a feed hole 303 of the separator, and flows back to the separator 3 for gas-;
step 2: the separated hydrogen chloride gas is discharged from a gas outlet 301 of the separator and then enters a pre-reactor mixing chamber 208 through a pre-reactor gas inlet 209, and the chloride solution in the separator 3 enters the main reactor 1 again through the circulating pump to continue to react;
when the concentration of the dichloropinacolone in the chlorination liquid in the separator 3 reaches more than 97 percent, the chlorination liquid is pumped out through a discharge pump and sent to dehydrochlorination equipment, hydrogen chloride gas dissolved in the chlorination liquid is removed under vacuum, the solution is cooled and crystallized into the dichloropinacolone, and the hydrogen chloride is absorbed into hydrochloric acid by water;
and step 3: free chlorine carried by hydrogen chloride gas reacts in the pre-reactor 2 (the reaction temperature is 42, the reaction pressure is 165KPa) and rises to a pre-reactor separation chamber 204, the free chlorine is mixed with pinacolone added from a pinacolone feed inlet 202, the carried liquid is recovered, the hydrogen chloride gas is discharged from a pre-reactor discharge port 203 and enters a demister, and the hydrogen chloride gas is cooled by cooling water in a pre-reactor shell side 201 during the reaction of the pre-reactor 2;
and 4, step 4: the demister traps hydrogen chloride liquid drops carried in the hydrogen chloride gas, and the hydrogen chloride gas enters hydrogen chloride absorption equipment;
and 5: the hydrogen chloride liquid drops separated in the demister and the mixed liquid discharged from the discharge port 302 of the separator are converged and then pumped into the main reactor 1 through a circulating pump.
It is obvious to a person skilled in the art that the invention is not restricted to details of the above-described exemplary embodiments, but that it can be implemented in other specific forms without departing from the spirit or essential characteristics of the invention. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Claims (5)
1. The utility model provides a device of differential circulation continuous production dichloro pinacolone, includes main reactor, pre-reactor, separator, circulating pump, discharge pump, defroster and pipeline and automatic control instrument, its characterized in that: the main reactor is a tubular microchannel reaction heat exchanger and is provided with a plurality of longitudinal main reactor tube sides and a plurality of transverse main reactor shell sides, two ends of each main reactor shell side are respectively connected with a main reactor cooling water inlet and a main reactor cooling water outlet which are arranged on two sides of the main reactor, a gas-liquid mixing chamber is arranged at the bottom of the main reactor, a main reactor gas inlet is formed in the bottom of the gas-liquid mixing chamber, a main reactor liquid inlet is formed in the side surface of the main reactor, a high-efficiency mixing structure body is arranged in the gas-liquid mixing chamber, a gas distributor is arranged in the middle of the main reactor, a main reactor chlorine inlet is formed in the gas distributor, and the upper end and the lower end of each main reactor tube side are respectively connected with a main reactor discharge port;
the pre-reactor is a tubular micro-channel reaction heat exchanger and is provided with a plurality of longitudinal pre-reactor tube passes and a plurality of transverse pre-reactor shell passes, the upper end in the pre-reactor is provided with a filler tower section, the two ends of the pre-reactor shell passes are respectively connected with a pre-reactor cooling water inlet and a pre-reactor cooling water outlet which are arranged at the two sides of the pre-reactor, the bottom of the pre-reactor is provided with a pre-reactor mixing chamber, the bottom of the pre-reactor mixing chamber is provided with a pre-reactor mixed liquid outlet, the side surface of the pre-reactor is provided with a pre-reactor gas inlet, the top of the pre-reactor is provided with a pre-reactor separation chamber, the side surface of the pre-;
the top of the separator is provided with a separator feeding port and a separator air outlet, and the bottom of the separator is provided with a separator chlorine inlet and a separator discharge port;
gaseous entry of main reactor and the gaseous entry of main reactor let in chlorine, and the separator pan feeding mouth is connected to the main reactor discharge gate, the gaseous entry linkage separator gas outlet of pre-reactor, the entry of defroster is connected to the discharge gate of pre-reactor, and the export liquid phase of defroster is connected and the circulating pump entry, and hydrogen chloride absorption equipment is connected to the gaseous phase, and the exit linkage main reactor liquid entry of circulating pump, separator chlorine import let in chlorine, and the entry of circulating pump and the entry of ejection of compact pump are connected to the separator discharge gate, the exit linkage splitter of ejection of compact pump.
2. The differential circulation continuous production dichloro pinacolone's device of claim 1, characterized by that: the main reactor tube side and the pre-reactor tube side are both filled with micro-channel ceramic filler, the diameter of the micro-channel ceramic filler is 8-100 mm, the diameter of the main reactor tube side is 10-110 mm, and the diameter of the pre-reactor tube side is 8-120 mm.
3. The differential circulation continuous production dichloro pinacolone's device of claim 2, characterized by that: the diameter of the micro-channel ceramic filler is 14-64 mm, the diameter of a main reactor tube side is 15-65 mm, and the diameter of a pre-reactor tube side is 30-100 mm.
4. The differential circulation continuous production dichloro pinacolone's device of claim 1, characterized by that: the main bodies of the main reactor and the pre-reactor are made of one or more of titanium alloy, impregnated graphite, carbon steel and silicon carbide, and the shells of the main reactor and the pre-reactor are made of carbon steel.
5. The differential circulation continuous production dichloro pinacolone's device of claim 1, characterized by that: the top of the separator is provided with a separator return port which is connected with a pre-reactor mixed liquid outlet.
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| CN201920452623.0U CN209906674U (en) | 2019-04-04 | 2019-04-04 | Device for continuously producing dichloropinacolone by differential circulation |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109912395A (en) * | 2019-04-04 | 2019-06-21 | 杭州众立化工科技有限公司 | A kind of device and process of differential circulation continuous production dichloro pinacolone |
| CN113663483A (en) * | 2021-10-22 | 2021-11-19 | 南通鸿富达利化工有限公司 | Tail gas recovery equipment used in pinacolone production process |
-
2019
- 2019-04-04 CN CN201920452623.0U patent/CN209906674U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109912395A (en) * | 2019-04-04 | 2019-06-21 | 杭州众立化工科技有限公司 | A kind of device and process of differential circulation continuous production dichloro pinacolone |
| CN113663483A (en) * | 2021-10-22 | 2021-11-19 | 南通鸿富达利化工有限公司 | Tail gas recovery equipment used in pinacolone production process |
| CN113663483B (en) * | 2021-10-22 | 2021-12-28 | 南通鸿富达利化工有限公司 | Tail gas recovery equipment used in pinacolone production process |
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Inventor after: Qiu Zhenzhong Inventor after: Wang Meizhen Inventor after: Wang Zhenhua Inventor before: Qiu Zhenzhong Inventor before: Wang Meizhen Inventor before: Wang Zhenhua |