CN207391316U - A kind of butyl acrylate heavy constituent cracking system - Google Patents
A kind of butyl acrylate heavy constituent cracking system Download PDFInfo
- Publication number
- CN207391316U CN207391316U CN201721349669.7U CN201721349669U CN207391316U CN 207391316 U CN207391316 U CN 207391316U CN 201721349669 U CN201721349669 U CN 201721349669U CN 207391316 U CN207391316 U CN 207391316U
- Authority
- CN
- China
- Prior art keywords
- butyl acrylate
- cracking
- heavy constituent
- tank
- cracking still
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A kind of butyl acrylate heavy constituent cracking system belongs to heavy constituent cracking field.It is characterized in that：Catalyst preparation tank（5）Bottom passes through catalyst output pipe（10）It is connected to cracking still（1）Lower part, cracking still（1）Top is connected with condenser by vapor delivery line（2）, condenser（2）Connection distillates material collecting tank（3）, distillate material collecting tank（3）Bottom is equipped with and distillates material output pipe（9）, cracking still（1）On be connected with middle pressure steam pipeline（11）.The system can significantly improve butyl acrylate heavy constituent cracking yield, so as to achieve the purpose that reduce butyl acrylate consumption acrylic acid and consumption n-butanol, the device operating method flexible and convenient, to the consumption reduction effect of butyl acrylate clearly.
Description
Technical field
A kind of butyl acrylate heavy constituent cracking system belongs to heavy constituent cracking field.
Background technology
Part heavy constituent waste oil can be generated in butyl acrylate device, the main component of butyl acrylate heavy constituent is β-fourth
Oxygroup butyl propionate, Beta-Butoxy butyl propionate can be analyzed to butyl acrylate and n-butanol at high temperature.It will with middle pressure steam
Butyl acrylate heavy constituent heats in cracking still, and Beta-Butoxy butyl propionate is made to be decomposed into butyl acrylate and just at high temperature
Butanol, while acrylic acid and PTSA are added into cracking still according to a certain percentage, make what the cracking of Beta-Butoxy butyl propionate generated
Acrylic acid synthesizing butyl ester, butyl acrylate steam in cracking still at high temperature under the effect of the catalyst for n-butanol and acrylic acid
Hair, butyl acrylate gas by condenser it is cold it is interior after, into material collecting tank is distillated, the material in distillate collecting tank passes through
Pipeline gets to acrylic acid and ester apparatus tank field crude acrylic acid butyl ester storage tank, recycles butyl acrylate therein.Cracking generates useless
Slag is got to incinerator by pipeline and is burned, and carries out harmless treatment.
The butyl acrylate heavy constituent generated at present in butyl acrylate production process is difficult to handle, and generally takes export trade
Mode is handled, and for existing butyl acrylate heavy constituent cracking yield generally 60% or so, this results in butyl acrylate in industry
Acrylic acid and n-butanol are consumed all in more than 600kg/h, are consumed higher.
Utility model content
The technical problems to be solved in the utility model is：Third can be significantly improved by overcoming the deficiencies of the prior art and provide one kind
The cracking yield of olefin(e) acid butyl ester heavy constituent reduces consumption, the butyl acrylate heavy constituent cracking system of energy-saving and emission-reduction.
Technical solution is used by the utility model solves its technical problem：Butyl acrylate heavy constituent cracking system
System, it is characterised in that：Including cracking still, catalyst preparation tank, the catalyst preparation pot bottom passes through catalyst efferent duct
Road is connected to cracking still lower part, and cracking still top is equipped with butyl acrylate heavy constituent feeding pipe, passes through gas phase at the top of cracking still
Pipeline is connected with condenser, and condenser connection distillates material collecting tank, distillates material collecting tank bottom and is exported equipped with material is distillated
Pipeline is connected with middle pressure steam pipeline on cracking still, and cracking still bottom connects residue tank by pipeline, and residue pot bottom is equipped with residual
Slag discharging pipeline.
, for improving the system of butyl acrylate heavy constituent cracking yield, cracking still top gas phase pipeline is connected with condensation for this
Mechanism, condensing mechanism are connected by pipeline with for storing the material collecting tank that distillates of distillate, distillate material collecting tank bottom
Equipped with material output pipe is distillated, material will be distillated and get to tank field crude acrylic acid fourth equipped with discharging pump by distillating material output pipe
Ester storage tank.Catalyst preparation tank cracks required catalyst and propylene for preparing butyl acrylate heavy constituent according to a certain percentage
Acid, catalyst preparation pot bottom have catalyst output pipe, and catalyst output pipe is equipped with catalyst and adds in pump, passes through catalysis
Agent adds in pump and adds catalyst and acrylic acid according to certain flow into cracking still, ensures that cracking still inner acrylic and n-butanol are normal
Reaction.The system can significantly improve butyl acrylate heavy constituent cracking yield, and butyl acrylate consumption acrylic acid is reduced so as to reach
And the purpose of consumption n-butanol, the device operating method flexible and convenient, to the consumption reduction effect of butyl acrylate clearly.
Beta-Butoxy butyl propionate content is very high in butyl acrylate heavy constituent, and direct export trade waste is larger, and existing
There is the low deficiency of cracking yield in cracking technology, cause butyl acrylate consumption acrylic acid and consumption n-butanol higher, add propylene
The cost of acid butyl ester.The low main cause of butyl acrylate heavy constituent cracking yield is the charging of cracking still inner acrylic butyl ester heavy constituent
Amount, acrylic acid inlet amount and PTSA addition proportions are improper or each inlet amount of cracking still and temperature control it is unstable,
Lytic effect is influenced, causes after cracking that Beta-Butoxy butyl propionate content is very high in residue, butyl acrylate contains in distillate
Amount is very low.Inventor has transformed butyl acrylate restructuring branch pipeline, increases the flowmeter and tune that can be fine-tuned on pipeline
Save valve.Increasing has the catalyst preparation tank of main-secondary tank structure, can accomplish continuously to cracking still for catalyst, and in catalyst
Increase the flowmeter that can be fine-tuned and regulating valve on output pipe, it can be ensured that add in the butyl acrylate restructuring of cracking still
Divide inlet amount, acrylic acid inlet amount and PTSA accurate in scale, suitable.Increase regulating valve on cracking still heating steam pipework, essence
Really control cracking still temperature, cracking still are connected to waste gas system by exhaust pipe, it is ensured that pressure stability exists in cracking still
101kPa or so, lytic effect is very good after taking more than measure.
Preferably, the material output pipe that distillates is equipped with discharging pump and valve.
Preferably, the cracking still is vertical tank, and the steam disc of connection medium pressure steam pipework is set inside cracking still
Pipe, cracking still are internally provided with blender, and middle pressure steam pipeline is equipped with the valve for control piper opening and closing.Ensure in cracking still
Material be heated evenly.
Preferably, the butyl acrylate heavy constituent feeding pipe is equipped with the valve for control piper opening and closing.
Preferably, the catalyst preparation tank is up and down by the main-secondary tank structure of apertured partition separation, the major trough on top
Mouth is added in equipped with acrylic acid charging line and catalyst PTSA, the secondary slot of lower part connects cracking still by catalyst output pipe.
Catalyst output pipe is equipped with catalyst and adds in pump, and add in pump by catalyst adds catalysis into cracking still according to certain flow
Agent and acrylic acid.
Preferably, the material collecting tank that distillates is horizontal tank.
Preferably, the residue tank is horizontal tank.
Preferably, residue discharging pipeline one end is connected to residue pot bottom, residue discharging pipeline other end connection
To incinerator；The residue tank is connected with pressue device.Residue tank pressurization will be cracked remaining residue by steam to get to
Incinerator is burned.
The condenser, which is arranged on, distillates material collecting tank top, condenser overhead and cracking still top gas phase outlet
Road connects, and condenser is connected with distillating material collecting tank, and the condensed product of condenser enters material collection tank.
The material output pipe that distillates is connected with distillating material collecting tank bottom, distillates and is set on material output pipe
There is discharging pump, distillate material output pipe and be equipped with the valve being opened and closed for control piper.
Compared with prior art, advantageous effect possessed by a kind of butyl acrylate heavy constituent cleavage method of the invention
It is：
1st, the system significantly improves cracking degree of the butyl acrylate heavy constituent in cracking still, can ensure cracking production
Object n-butanol fully reacts generation butyl acrylate with acrylic acid, and n-butanol is avoided to generate butyl oxide at high temperature, is passed through simultaneously
Intense adjustment controls suitable technological parameter that can be substantially reduced the content of Beta-Butoxy butyl propionate in distillate, makes propylene
Acid butyl ester yield reaches more than 85%.Since all state modulators are using automation control, it can not only reach the mesh accurately adjusted
, the labor intensity of worker is also reduced, greatly reduces the workload of worker's execute-in-place.
2nd, the system solves the problems, such as that residual material is more in butyl acrylate heavy constituent, has energy-saving effect
Fruit.The content of butyl acrylate greatly improves in distillate, the stabilization long period of the butyl acrylate device to recycling distillate
It runs significant.Compared to existing cracker yield 60% or so, yield of the present invention reaches more than 85%, can make propylene
Acid butyl ester consumes acrylic acid and n-butanol is down to below 585kg/t, and consumption reduction effect can reach more than 10kg/t, have prominent technology
Effect.
Description of the drawings
A kind of schematic diagrames of butyl acrylate heavy constituent cracking system of Fig. 1.
Wherein：1st, cracking still 2, condenser 3, distillate material collecting tank 4, discharging pump 5, catalyst preparation tank
6th, catalyst add in pump 7, residue tank 8, butyl acrylate heavy constituent feeding pipe 9, distillate material output pipe 10,
Catalyst output pipe 11, middle pressure steam pipeline 12, acrylic acid charging line 13, catalyst PTSA add in mouth 14,
Residue discharging pipeline.
Specific embodiment
Fig. 1 is a kind of for improving the most preferred embodiment of butyl acrylate heavy constituent cracking yield system of the present invention, under
With reference to attached drawing 1, the present invention will be further described in face.
With reference to Fig. 1, a kind of butyl acrylate heavy constituent cracking system of the invention, the present invention is by the following technical programs
It realizes：This is used for the system for improving butyl acrylate heavy constituent cracking yield, divides including being used to recombinate butyl acrylate
The cracking still 1 of solution, 1 top of cracking still are equipped with butyl acrylate heavy constituent feeding pipe 8, and it is defeated that 1 lower part of cracking still is equipped with catalyst
Go out pipeline 10,1 top gas phase pipeline of cracking still is connected with condenser 2, and condenser 2 stores evaporating for distillate by pipeline with being used for
Go out material collection tank 3 to connect, distillate 3 bottom of material collecting tank equipped with material output pipe 9 is distillated, distillate material output pipe 9
Material, which will be distillated, equipped with discharging pump 4 gets to tank field crude acrylic acid butyl ester storage tank；Catalyst preparation tank 5 is for according to a certain percentage
The catalyst and acrylic acid needed for the cracking of butyl acrylate heavy constituent are prepared, catalyst efferent duct is arranged at 5 bottom of catalyst preparation tank
Road 10, catalyst output pipe 10 are equipped with catalyst and add in pump 6, and pump 6 is added in into cracking still 1 according to certain by catalyst
Flow adds catalyst and acrylic acid, and cracking still 1 is equipped with middle pressure steam pipeline 11 and provides heat source for cracking still, ensures in cracking still 1
Acrylic acid and n-butanol normal reaction；Remaining residue enters residue tank 7 by pipeline after the cracking of butyl acrylate heavy constituent, residual
7 bottom of slag ladle, which is equipped with residue discharging pipeline 14 and will crack remaining residue and get to incinerator, burns.
It distillates material output pipe 9 and is connected with distillating 3 bottom of material collecting tank, distillate material output pipe 9 and be equipped with
Discharging pump 4 distillates material output pipe 9 and is equipped with the valve being opened and closed for control piper.
Cracking still 1 is vertical tank, and cracking still 1 is internally provided with steam pipe coil, by middle pressure steam pipeline 11 in cracking still 1
Butyl acrylate heavy constituent heated, cracking still）Blender is internally provided with, ensures that the material in cracking still is heated evenly,
Middle pressure steam pipeline 11 is equipped with the valve for control piper opening and closing.Butyl acrylate heavy constituent feeding pipe 8, which is equipped with, to be used
In the valve of control piper opening and closing.
Condenser 2, which is arranged on, distillates 3 top of material collecting tank, 2 top of condenser and 1 top gas phase export pipeline of cracking still
Connection, 2 lower part of condenser are connected with distillating material collecting tank 3, and the condensed product of condenser 2 enters material collection tank 3.It evaporates
Go out material collection tank 3 for horizontal tank, distillate 3 bottom of material collecting tank equipped with discharge port, discharge port connects discharging pump by pipeline
4。
Catalyst preparation tank 5 is main-secondary tank structure, adds in mouth 13 equipped with acrylic acid charging line 12 and catalyst PTSA, urges
Catalyst output pipe 10 is arranged at 5 bottom of agent preparing tank, and catalyst output pipe 10 is equipped with catalyst and adds in pump 6, by urging
Agent adds in pump 6 and adds catalyst and acrylic acid according to certain flow into cracking still, and catalyst output pipe 10 is equipped with and is used for
The valve of control piper opening and closing.
Residue tank 7 is horizontal tank, and residue tank 7 is set and 1 lower part of cracking still, and 1 bottom of cracking still is connected to residual equipped with pipeline
7 top of slag ladle, the residue after cracking are flow to residue tank 7 by gravity.Residue discharging pipeline 14 is connected to 7 bottom of residue tank,
Residue tank 7 pressurizeed by steam to crack remaining residue and get to incinerator and is burned, residue discharging pipeline 14 is equipped with
For the valve of control piper opening and closing.
The above-described operating method for being used to improve butyl acrylate heavy constituent cracking yield system, step are as follows：
a）Catalyst preparation tank 5 is main-secondary tank structure, and solvent is acrylic acid, solute PTSA, according to PTSA mass fractions
1.5% is configured.
b）According to 1:4 ratio adds in catalyst solution and butyl acrylate heavy constituent into cracking still 1, prepares cracking
Material controls steam addition by the regulating valve on middle pressure steam pipeline 11, adjusts the temperature in cracking still 1 as 175 ~ 185 DEG C,
1 system of cracking still is connected with waste line, and it is atmospheric pressure to control in cracking still 1 pressure, main in butyl acrylate heavy constituent
Ingredient Beta-Butoxy butyl propionate is cracked into butyl acrylate and n-butanol with this condition.
C) butyl acrylate heavy constituent continues into cracking still 1 by butyl acrylate heavy constituent feeding pipe 8, and flow is
500 ~ 700kg/h, catalyst and acrylic acid continue into cracking still 1 by catalyst output pipe 10, and flow is 120 ~ 175
Kg/h, the n-butanol that the cracking of butyl acrylate heavy constituent generates is with adding in the acrylic acid of cracking still under catalyst and hot conditions
Reaction generation butyl acrylate.
d）Gas phase distillate in cracking still 1 becomes liquid after the condensation of condenser 2, into distillating material collecting tank
3, it is 25 ~ 35 DEG C to distillate temperature in material collecting tank 3.
E) by distillating the discharging pump 4 on material output pipe 9, the material distillated in material collecting tank 3 is got into centre
Tank field crude acrylic acid butyl ester storage tank is recycled.
F) residue after cracking in cracking still 1 is flow to residue tank 7 by gravity, by steam by residue tank 7 pressurize by
Residue is got to incinerator and is burned.
The course of work and effect are further illustrated by example 1 below ~ 3.
Embodiment 1
a）Prepare catalyst：To catalyst preparation tank（5）Acrylic acid is inside filled, adding in PTSA according to mass fraction 1.5% prepares
Catalyst solution.According to 1:4 ratio is to cracking still（1）Interior addition catalyst solution and butyl acrylate heavy constituent.
b）Cracking：Pass through middle pressure steam pipeline（11）On regulating valve control steam addition, adjust cracking still（1）Interior
Temperature is 175 ~ 185 DEG C, cracking still（1）System is connected with waste line, controls cracking still（1）Interior pressure be atmospheric pressure, propylene
Main component Beta-Butoxy butyl propionate in acid butyl ester heavy constituent is cracked into butyl acrylate and n-butanol third with this condition
Olefin(e) acid butyl ester heavy constituent passes through butyl acrylate heavy constituent feeding pipe feeding pipe（8）Continue into cracking still（1）, flow is
500 ~ 700kg/h, catalyst and acrylic acid pass through catalyst output pipe（10）Continue into cracking still（1）, flow for 120 ~
175 kg/h, the n-butanol that the cracking of butyl acrylate heavy constituent generates react generation with acrylic acid under catalyst and hot conditions
Butyl acrylate.
C) condense：Cracking still（1）In gas phase distillate pass through condenser（2）After condensation, become liquid, into distillate
Expect collecting tank（3）, distillate material collecting tank（3）Middle temperature is 25 ~ 35 DEG C.Pass through discharging pump（4）Distillate is got into pans
Area's crude acrylic acid butyl ester storage tank is recycled.
Embodiment 2
a）Prepare catalyst：To catalyst preparation tank（5）Acrylic acid is inside filled, adding in PTSA preparations according to mass fraction 1% urges
Agent solution.According to 1:5 ratio is to cracking still（1）Interior addition catalyst solution and butyl acrylate heavy constituent.
b）Cracking：Pass through middle pressure steam pipeline（11）On regulating valve control steam addition, adjust cracking still（1）Interior
Temperature is 175 ~ 185 DEG C, cracking still（1）System is connected with waste line, controls cracking still（1）Interior pressure be atmospheric pressure, propylene
Main component Beta-Butoxy butyl propionate in acid butyl ester heavy constituent is cracked into butyl acrylate and n-butanol third with this condition
Olefin(e) acid butyl ester heavy constituent passes through butyl acrylate heavy constituent feeding pipe feeding pipe（8）Continue into cracking still（1）, flow is
500 ~ 700kg/h, catalyst and acrylic acid pass through catalyst output pipe（10）Continue into cracking still（1）, flow for 100 ~
140 kg/h, the n-butanol that the cracking of butyl acrylate heavy constituent generates react generation with acrylic acid under catalyst and hot conditions
Butyl acrylate.
C) condense：Cracking still（1）In gas phase distillate pass through condenser（2）After condensation, become liquid, into distillate
Expect collecting tank（3）, distillate material collecting tank（3）Middle temperature is 25 ~ 35 DEG C.Pass through discharging pump（4）Distillate is got into pans
Area's crude acrylic acid butyl ester storage tank is recycled.
Embodiment 3
a）Prepare catalyst：To catalyst preparation tank（5）Acrylic acid is inside filled, adding in PTSA preparations according to mass fraction 2% urges
Agent solution.According to 1:6 ratio is to cracking still（1）Interior addition catalyst solution and butyl acrylate heavy constituent.
b）Cracking：Pass through middle pressure steam pipeline（11）On regulating valve control steam addition, adjust cracking still（1）Interior
Temperature is 175 ~ 185 DEG C, cracking still（1）System is connected with waste line, controls cracking still（1）Interior pressure be atmospheric pressure, propylene
Main component Beta-Butoxy butyl propionate in acid butyl ester heavy constituent is cracked into butyl acrylate and n-butanol third with this condition
Olefin(e) acid butyl ester heavy constituent passes through butyl acrylate heavy constituent feeding pipe feeding pipe（8）Continue into cracking still（1）, flow is
500 ~ 700kg/h, catalyst and acrylic acid pass through catalyst output pipe（10）Continue into cracking still（1）, flow for 85 ~
120 kg/h, the n-butanol that the cracking of butyl acrylate heavy constituent generates react generation with acrylic acid under catalyst and hot conditions
Butyl acrylate.
C) condense：Cracking still（1）In gas phase distillate pass through condenser（2）After condensation, become liquid, into distillate
Expect collecting tank（3）, distillate material collecting tank（3）Middle temperature is 25 ~ 35 DEG C.Pass through discharging pump（4）Distillate is got into pans
Area's crude acrylic acid butyl ester storage tank is recycled.
Performance test is tested
In Statistics Implementation example 1 ~ 3：Monthly butyl acrylate heavy constituent feed pipe is counted in units of ton（8）Add in cracking still
（1）Butyl acrylate heavy constituent gross mass, total matter of butyl acrylate in the monthly distillate of output is counted in units of ton
Amount.Pass through " monthly the butyl crotonate heavy constituent of butyl acrylate total output/monthly feeds gross mass " calculating " butyl acrylate weight
Component cracks yield ", each embodiment continuously records 6 months, takes the average value of " butyl acrylate heavy constituent cracks yield ".
1 embodiment of table, 1 ~ 3 the performance test results
。
It can be seen that butyl acrylate heavy constituent cracks yield and is significantly improved compared with prior art by data above, and
Without apparent peculiar smell in its exterior working environment in 1 ~ 3 production process of embodiment, hence it is evident that improve production environment.
The above descriptions are merely preferred embodiments of the present invention, is not to make other forms to the utility model
Limitation, any person skilled in the art is changed or is modified as possibly also with the technology contents of the disclosure above equivalent
The equivalent embodiment of variation.But it is every without departing from the content of the technical scheme of the utility model, the technology according to the utility model is real
Any simple modification, equivalent variations and the remodeling that confrontation above example is made still fall within the guarantor of technical solutions of the utility model
Protect scope.
Claims (8)
1. a kind of butyl acrylate heavy constituent cracking system, it is characterised in that：Including cracking still（1）, catalyst preparation tank（5）,
The catalyst preparation tank（5）Bottom passes through catalyst output pipe（10）It is connected to cracking still（1）Lower part, cracking still（1）
Top is equipped with butyl acrylate heavy constituent feeding pipe（8）, cracking still（1）Top is connected with condenser by vapor delivery line（2）,
Condenser（2）Connection distillates material collecting tank（3）, distillate material collecting tank（3）Bottom is equipped with and distillates material output pipe（9）,
Cracking still（1）On be connected with middle pressure steam pipeline（11）, cracking still（1）Bottom connects residue tank by pipeline（7）, residue tank
（7）Bottom is equipped with residue discharging pipeline（14）.
2. a kind of butyl acrylate heavy constituent cracking system according to claim 1, it is characterised in that：The distillate
Expect output pipe（9）It is equipped with discharging pump（4）And valve.
3. a kind of butyl acrylate heavy constituent cracking system according to claim 1, it is characterised in that：The cracking still
（1）For vertical tank, cracking still（1）Inside sets connection medium pressure steam pipework（11）Steam pipe coil, cracking still（1）Inside is set
There are blender, middle pressure steam pipeline（11）It is equipped with the valve for control piper opening and closing.
4. a kind of butyl acrylate heavy constituent cracking system according to claim 1, it is characterised in that：The acrylic acid
Butyl ester heavy constituent feeding pipe（8）It is equipped with the valve for control piper opening and closing.
5. a kind of butyl acrylate heavy constituent cracking system according to claim 1, it is characterised in that：The catalyst
Preparing tank（5）For the main-secondary tank structure separated up and down by apertured partition, the major trough on top is equipped with acrylic acid charging line（12）With
Catalyst PTSA adds in mouth（13）, the secondary slot of lower part passes through catalyst output pipe（10）Connect cracking still（1）.
6. a kind of butyl acrylate heavy constituent cracking system according to claim 1, it is characterised in that：The distillate
Expect collecting tank（3）For horizontal tank.
7. a kind of butyl acrylate heavy constituent cracking system according to claim 1, it is characterised in that：The residue tank
（7）For horizontal tank.
8. a kind of butyl acrylate heavy constituent cracking system according to claim 1, it is characterised in that：The residue goes out
Expects pipe road（14）One end is connected to residue tank（7）Bottom, residue discharging pipeline（14）The other end is connected to incinerator；Described is residual
Slag ladle（7）It is connected with pressue device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721349669.7U CN207391316U (en) | 2017-10-19 | 2017-10-19 | A kind of butyl acrylate heavy constituent cracking system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721349669.7U CN207391316U (en) | 2017-10-19 | 2017-10-19 | A kind of butyl acrylate heavy constituent cracking system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207391316U true CN207391316U (en) | 2018-05-22 |
Family
ID=62328809
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201721349669.7U Active CN207391316U (en) | 2017-10-19 | 2017-10-19 | A kind of butyl acrylate heavy constituent cracking system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207391316U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109942424A (en) * | 2019-04-19 | 2019-06-28 | 泰兴金江化学工业有限公司 | A kind of n-butyl acrylate heavy constituent recovery process and device |
| CN113262704A (en) * | 2021-05-27 | 2021-08-17 | 聊城鲁西多元醇新材料科技有限公司 | Cracking catalyst preparation system and method and application thereof |
| CN114716316A (en) * | 2022-03-23 | 2022-07-08 | 卫星化学股份有限公司 | Semi-continuous acrylic acid and ester heavy component recovery process |
-
2017
- 2017-10-19 CN CN201721349669.7U patent/CN207391316U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109942424A (en) * | 2019-04-19 | 2019-06-28 | 泰兴金江化学工业有限公司 | A kind of n-butyl acrylate heavy constituent recovery process and device |
| CN113262704A (en) * | 2021-05-27 | 2021-08-17 | 聊城鲁西多元醇新材料科技有限公司 | Cracking catalyst preparation system and method and application thereof |
| CN114716316A (en) * | 2022-03-23 | 2022-07-08 | 卫星化学股份有限公司 | Semi-continuous acrylic acid and ester heavy component recovery process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN207391316U (en) | A kind of butyl acrylate heavy constituent cracking system | |
| CN101691495A (en) | Method and device for preparing bio-oil and chemicals by pyrolyzing biomass in steps | |
| CN104673340A (en) | Systematic device and method for biomass microwave pyrolysis poly-generation by adopting combined washing and baking pretreatment | |
| CN105154114A (en) | Device and method for preparing biochar by using Chinese medicinal materials and waste generated during traditional Chinese medicine production process | |
| CN104910931B (en) | A kind of farm's solid waste continuous pyrolysis carbonizing treatment method and device | |
| CN106753482B (en) | A kind of biomass pyrolytic-catalytic cracking preparing aromatic hydrocarbon integrated reacting device and application method | |
| CN108840548A (en) | Pyrohydrolysis flash separation device and pyrohydrolysis flash separation technique, pyrohydrolysis system and pyrohydrolysis technique | |
| CN101613617B (en) | Method for preparing biological oil through vacuum pyrolysis of biomasses | |
| CN202193756U (en) | Biomass microwave pyrolysis circulating treatment equipment | |
| CN102853455A (en) | Biomass heating and drying furnace | |
| CN102443407B (en) | Crude oil deep drawing process method | |
| CN103013817A (en) | Liquefaction equipment and liquefaction process for producing alcohol by using starchiness as raw material | |
| CN206927864U (en) | A kind of hydro-thermal process improves the device of low-order coal water coal slurry concentration | |
| CN1923952A (en) | Collection method of bamboo vinegar stock solution | |
| CN201598271U (en) | Decoking and dust removing equipment utilizing garbage microwave pyrolysis gas to prepare fuel gas | |
| CN208844047U (en) | A kind of wine brewing distillation equipment | |
| CN102517061A (en) | Equipment for treating non-sticky coal and coking method for treating non-sticky coal | |
| CN101974363B (en) | Method for recovering and treating waste industrial oil and equipment for implementing method | |
| CN207227373U (en) | A kind of plant medicinal liquid extraction and Activated Carbon Production process equipment | |
| CN207243819U (en) | A kind of system that tar slag is handled by totally-enclosed anaerobic cracking reaction | |
| CN102703123A (en) | Biomass particle gasification process for kiln | |
| CN202161827U (en) | Gooseneck-typed distilling device for purifying spice | |
| CN201530793U (en) | Energy saving apparatus in hard carbon black production | |
| CN206721114U (en) | Straw recycles chemical plant installations | |
| CN201825927U (en) | Condenser for separating biomass cracking gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |