CN206438057U - The system that isobutene is prepared for tert-butyl alcohol dehydration - Google Patents
The system that isobutene is prepared for tert-butyl alcohol dehydration Download PDFInfo
- Publication number
- CN206438057U CN206438057U CN201720082568.1U CN201720082568U CN206438057U CN 206438057 U CN206438057 U CN 206438057U CN 201720082568 U CN201720082568 U CN 201720082568U CN 206438057 U CN206438057 U CN 206438057U
- Authority
- CN
- China
- Prior art keywords
- reaction tower
- conveying pipeline
- point
- flow container
- tower
- 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
Abstract
The utility model discloses a kind of system for preparing isobutene for tert-butyl alcohol dehydration, including first module and second unit；First module includes the first condenser, primary heater, the first reaction tower, the first reboiler and first point of flow container；Second unit includes the second condenser, secondary heater, the second reaction tower, the second reboiler and second point of flow container；The bottom of primary heater is provided with the first conveying pipeline and the second conveying pipeline, is respectively used at least part question response raw material from primary heater sending into the first reaction tower and the second reaction tower；The bottom of first point of flow container is provided with the 3rd conveying pipeline and the 4th conveying pipeline, 3rd conveying pipeline is used to deliver to the first reaction tower using at least part liquid phase isolated through first point of flow container as overhead reflux, and the 4th conveying pipeline is used at least part liquid phase isolated through first point of flow container delivering to secondary heater.The system can need free switching series and parallel production model according to production, flexibly.
Description
Technical field
The utility model belongs to the preparation field of isobutene, particularly a kind of to be for what tert-butyl alcohol dehydration prepared isobutene
System.
Background technology
Isobutene is a kind of important basic organic chemical industry raw material, is one of monomer of synthetic rubber, its chemical utilization way
Footpath mainly includes two kinds of utilization and the high-purity isobutene processing and utilization of C4 raffinate isobutenes, and the former is mainly for the production of methyl- tert fourth
Base ether and the tert-butyl alcohol, the latter can be used for a variety of Organic Chemicals such as production butyl rubber, polyisobutene and methacrylate
And fine chemicals.The method of production high-purity isobutylene mainly has methyl tertiary butyl ether(MTBE) cracking process and tert-butyl alcohol dehydration at present
Method.
Methyl tertiary butyl ether(MTBE) cracking process product purity is high, and unit scale flexibility is big, can produce first according to the market demand
The tertiary butyl ether of base or isobutene, but be due to that etherification method side reaction is more, to obtain high-purity isobutylene product, separation and purification technique is answered
Miscellaneous, long flow path, energy consumption is big.The technological process of tert-butyl alcohol dehydration method is simple, and reaction condition is gentle, and side reaction is few, and separation and purification is easy,
Product quality is high, and equipment investment is few.Two kinds of techniques are compared, production unit isobutene product, and tert-butyl alcohol dehydration method is than methyl- tert fourth
Base ether-splitting solution is more economical.
Disclosed in the A of patent CN 104447167 using the raw material tert-butyl alcohol and from isobutene tower bottom of rectifying tower produce with
The tert-butyl alcohol and water vaporize separation for the mixed liquor of Main Ingredients and Appearance in vaporization stripping tower, the tert-butyl alcohol and the water mixing come out from tower top
Steam sends into tert-butyl alcohol dehydration reaction system, and the isobutene gas obtained after reaction is sent out.It is public in the A of patent CN 101381273
Open and the raw material tert-butyl alcohol is continuously added to the reactor equipped with superpower solid acid catalyst, and heating is allowed to boiling cracking, cracking
The isobutene gas of generation flows into knockout tower together with boiling tert-butyl alcohol gas and separated, and isobutene gas flows out from tower top,
The unreacted tert-butyl alcohol is in overhead condensation partial reflux tower, and part outflow is back to reactor.The two patent former concerns
The gasification of the tert-butyl alcohol, the separation of the latter's concern product isobutene and the tert-butyl alcohol, therefore all employ the side that reactor is combined with tower
Formula, adds the input and operating cost of equipment；Process units involved by the two patents is one-pot, single column mode operation,
Production capacity regulation is dumb.
Utility model content
The purpose of this utility model is to provide a kind of system for preparing isobutene for tert-butyl alcohol dehydration, and the system can be with
Isobutene is prepared with tert-butyl alcohol dehydration, and can flexibly select different mode according to actual needs.
To realize the purpose of this utility model, the utility model uses following technical scheme：
A kind of system for preparing isobutene for tert-butyl alcohol dehydration, including first module and second unit；
The first module includes the first condenser, primary heater, the first reaction tower, the first reboiler and first point of liquid
Tank；The second unit includes the second condenser, secondary heater, the second reaction tower, the second reboiler and second point of flow container；Its
In,
The raw material tert-butyl alcohol that first condenser is used for the overhead product and question response for making first reaction tower exchanges heat
Cooling；
The primary heater is used to make the question response raw material heat absorption heating from first condenser；Described first adds
The bottom of hot device is provided with the first conveying pipeline and the second conveying pipeline, and the first conveying pipeline is provided with the first valve, described
First conveying pipeline is used at least part question response raw material from the primary heater sending into first reaction tower；Institute
The second conveying pipeline is stated provided with the second valve, the second conveying pipeline is used at least portion from the primary heater
Question response raw material is divided to send into second reaction tower；
First reaction tower is used to receive the question response raw material from the first conveying pipeline and is dehydrated it
Reaction prepares isobutene；
First reboiler is used to make the tower bottom product heating of first reaction tower to boil again；
First point of flow container is used to receive the overhead product from first condenser and carries out gas-liquid separation to it；
The bottom of first point of flow container is provided with the 3rd conveying pipeline and the 4th conveying pipeline, and the 3rd conveying pipeline is provided with the
Three valves, the 3rd conveying pipeline is used to regard at least part liquid phase isolated through first point of flow container as overhead reflux
Deliver to first reaction tower；The 4th conveying pipeline is provided with the 4th valve, and the 4th conveying pipeline is used for will be through institute
State at least part liquid phase that first point of flow container isolate and deliver to the secondary heater；
The secondary heater is used to make the material heat absorption heating from the 4th conveying pipeline, to obtain the thing that heats up
Material；
Second reaction tower is used to receive the heating material from the secondary heater with coming from second conveying
The question response raw material of pipeline, and its progress dehydration is prepared isobutene；
Second reboiler is used to make the tower bottom product heating of second reaction tower to boil again；
Second condenser is used to receive the overhead product from second reaction tower and it is condensed, with
To condensation material；
Second point of flow container is used to carry out gas-liquid separation to the condensation material from second condenser；Described second
The bottom of point flow container is provided with the 5th conveying pipeline, at least part liquid phase for will being isolated through second point of flow container as
Overhead reflux is inputted in second reaction tower.
Preferably, the primary heater is used to making question response raw material from first condenser and described first anti-
Answer the tower bottom product of tower to exchange heat to heat up.
Preferably, the secondary heater is used to make material and second reaction tower from the 4th conveying pipeline
Tower bottom product heat exchange heating.
Preferably, first reaction tower and second reaction tower include column plate section from the bottom to top and filler respectively
Section, the number of plates of the column plate section is 15-35, and the filler number of plies of the packing section is 2-8, first reaction tower and described the
The charging aperture of two reaction towers is arranged at from the 1/2 of the column plate section to the top of the packing section.
Preferably, the top exit of first point of flow container is provided with the first product output line, described for that will come from
The top product output of first point of flow container；The top exit of second point of flow container is provided with the second product output line, is used for
By the top product output from second point of flow container.
The beneficial effects of the utility model are：
(1) system of the present utility model for preparing isobutene for tert-butyl alcohol dehydration, can according to different production needs,
By controlling different valves, different production processes are realized；Such as, when needing to improve the conversion ratio of the tert-butyl alcohol, the is opened
One valve 91 and the 4th valve 121, close the second valve 101 and the 3rd valve 111, first module 01 and second unit 02 is gone here and there
Connection connection, and then improve the conversion ratio of the tert-butyl alcohol；When needing to improve production capacity, the first valve 91, the second valve 101 and the are opened
Three valves 111, close the 4th valve 121, are connected in parallel first module 01 and second unit 02, to improve production capacity；Two kinds of moulds
Formula can produce regulation space greatly, can meet different production requirements according to production requirement free switching；And can in using anti-
The heat entrained by material after answering is heated to charging, while the purpose cooled to reacted material is also reached,
The use of steam and cooling water can be reduced, the purpose for saving the energy is reached；
(2) by the setting to secondary heater 2 ', effectively the bottom of towe from the second reaction tower 3 ' can not only be utilized to produce
Heat entrained by thing (t butanol content i.e. positioned at bottom of towe is less than 2ppm t-butanol solution) enters to the second reaction tower 3 '
Material (material from the 4th conveying pipeline 12) is heated, while can also reach to the bottom of towe from the second reaction tower 3 '
The purpose that product is cooled, further reduces the use of steam and cooling water, reaches the purpose for saving the energy；
(3) by the setting to primary heater 2, the tower bottom product from the first reaction tower 3 can be effectively utilized (to ascend the throne
T butanol content in bottom of towe is less than 2ppm t-butanol solution) entrained by charging of the heat to the first reaction tower 3 added
Heat, while reach the purpose cooled to the tower bottom product of the first reaction tower 3, further reduces making for steam and cooling water
With, reach save the energy purpose.
Brief description of the drawings
Fig. 1 prepares the structure of the system of isobutene in one embodiment to be of the present utility model for tert-butyl alcohol dehydration
Schematic diagram.
Embodiment
The technical solution of the utility model and its effect are described further below by way of embodiment.Following reality
The mode of applying is merely to illustrate content of the present utility model, is not limited to protection domain of the present utility model.Using this practicality
The simple change that new design is carried out to the utility model is all in the scope that the utility model is claimed.
As shown in figure 1, the system of the present utility model for preparing isobutene for tert-butyl alcohol dehydration, including the He of first module 01
Second unit 02；
The first module 01 includes the first condenser 1, primary heater 2, the first reaction tower 3, the first reboiler 4 and the
One point of flow container 5；The second unit 02 includes the second condenser 1 ', secondary heater 2 ', the second reaction tower 3 ', the second reboiler
4 ' and second point of flow container 5 '；Wherein,
First condenser 1 is used to change the overhead product of first reaction tower 3 and the raw material tert-butyl alcohol of question response
Heat cooling；
The primary heater 2 is used to make the question response raw material heat absorption heating from first condenser 1；Described first
The bottom of heater 2 is provided with the first conveying pipeline 9 and the second conveying pipeline 10, and the first conveying pipeline 9 is provided with the first valve
Door 91, the first conveying pipeline 9 is used at least part question response raw material feeding described the from the primary heater 2
One reaction tower 3；The second conveying pipeline 10 is provided with the second valve 101, and the second conveying pipeline 10 is used to that institute will to be come from
At least part question response raw material for stating primary heater 2 sends into second reaction tower 3 '；
First reaction tower 3 is used to receive the question response raw material from the first conveying pipeline 9 and is taken off it
Water reaction prepares isobutene；
First reboiler 4 is used to make the tower bottom product heating of first reaction tower 3 to boil again；
First point of flow container 5 is used to receive the overhead product from first condenser 1 and gas-liquid point is carried out to it
From；The bottom of first point of flow container 5 is provided with the 3rd conveying pipeline 11 and the 4th conveying pipeline 12, the 3rd conveying pipeline
11 are provided with the 3rd valve 111, and the 3rd conveying pipeline 11 is used at least part that will be isolated through first point of flow container 5
Liquid phase delivers to first reaction tower 3 as overhead reflux；The 4th conveying pipeline 12 is provided with the 4th valve 121, described
4th conveying pipeline 12 is used at least part liquid phase isolated through first point of flow container 5 delivering to the secondary heater
2’；
The secondary heater 2 ' is used to make the material heat absorption heating from the 4th conveying pipeline 12, to be heated up
Material；
Second reaction tower 3 ' is used to receive the heating material from the secondary heater 2 ' with coming from described second
The question response raw material of conveying pipeline 10, and its progress dehydration is prepared isobutene；
Second reboiler 4 ' is used to make the tower bottom product heating of second reaction tower 3 ' to boil again；
Second condenser 1 ' is used to receive the overhead product from second reaction tower 3 ' and it is condensed,
To obtain condensing material；
Second point of flow container 5 ' is used to carry out gas-liquid separation to the condensation material from second condenser 1 '；It is described
The bottom of second point of flow container 5 ' is provided with the 5th conveying pipeline 8, at least portion that will be isolated through second point of flow container 5 '
Liquid phase is divided to be inputted as overhead reflux in second reaction tower 3 '.
The system of the present utility model for preparing isobutene for tert-butyl alcohol dehydration, can lead to according to different production needs
Cross and control different valves, realize different production processes；Such as, when needing to improve the conversion ratio of the tert-butyl alcohol, first is opened
The valve 121 of valve 91 and the 4th, closes the second valve 101 and the 3rd valve 111, first module 01 and second unit 02 is connected
Connection, and then improve the conversion ratio of the tert-butyl alcohol；Under series model, tertiary fourth in the charging of the first reaction tower 3 and the second reaction tower 3 '
The concentration of alcohol is 94~98wt%, and the concentration of isobutene is 60~70wt% in tower top discharging；When needing to improve production capacity, open
First valve 91, the second valve 101 and the 3rd valve 111, close the 4th valve 121, make first module 01 and second unit 02
It is connected in parallel, to improve production capacity；Under paralleling model, the concentration of the tert-butyl alcohol is 94~98wt% in the charging of the first reaction tower 3, the
The concentration of the tert-butyl alcohol is 30~40wt% in the charging of two reaction towers 3 ', and isobutene is dense in the tower top discharging of the first reaction tower 3
Spend for 60~70wt%, the concentration of isobutene is 55~70wt% in the tower top discharging of the second reaction tower 3 '；Both of which can root
According to production requirement free switching, production regulation space is big, can meet different production requirements；And can in using reacted
Heat entrained by material is heated to charging, while also reaching the purpose cooled to reacted material, can be reduced
The use of steam and cooling water, reaches the purpose for saving the energy, such as charging is inputted into primary heater by the first condenser 1
Heated in 2, it is possible to use the heat entrained by the overhead product of the first reaction tower is heated to charging, while charging
Cooling effect is played to the overhead product of the first reaction tower, this can just reduce the use of steam and cooling water simultaneously, save energy
Source.
In one embodiment, the bottom temperature of the first reaction tower 3 and the second reaction tower 3 ' is 140-150 DEG C, such as
150℃。
In one embodiment, the feed rate of the charging of the first reaction tower 3 and the second reaction tower 3 ' is 180-
360kmol/hr, such as 300kmol/hr.
In one embodiment, the primary heater 2 is used to make the question response raw material from first condenser 1
Exchange heat and heat up with the tower bottom product of first reaction tower 3, to reduce the use of steam and cooling water simultaneously, save the energy.
In one embodiment, the secondary heater 2 ' be used to making material from the 4th conveying pipeline 12 with
The tower bottom product heat exchange heating of second reaction tower 3 ', to reduce the use of steam and cooling water simultaneously, saves the energy.
In one embodiment, first reaction tower 3 and second reaction tower 3 ' are included from the bottom to top respectively
Column plate section and packing section, the number of plates of the column plate section is 15-35, and the filler number of plies of the packing section is 2-8, and described first is anti-
The charging aperture of tower 3 and second reaction tower 3 ' is answered to be arranged at from the 1/2 of the column plate section to the top of the packing section, from
And charging is fully contacted with packing section catalyst, be conducive to gas-liquid after dehydration to be separated.
In one embodiment, the top exit of first point of flow container 5 is provided with the first product output line 7, uses
Exported in by the top product from first point of flow container 5；The top exit of second point of flow container 5 ' is provided with the second production
Thing export pipeline 7 ', for the top product from second point of flow container 5 ' to be exported.
Equipment involved by the utility model is the common equipment of this area.
The running of the system of the present utility model for preparing isobutene for tert-butyl alcohol dehydration is as follows：
Series model：
The first valve 91 and the 4th valve 121 are opened, the second valve 101 and the 3rd valve 111 is closed, makes first module 01
It is connected in series with second unit 02, charging t-butanol solution (concentration is 94~98wt%) adds through the first condenser 1 input first
It is heated in hot device 2 after 100 DEG C, is inputted in the first reaction tower 3, entered through charging aperture with certain flow (such as 300kmol/hr)
Row tert-butyl alcohol dehydration reacts；And tower bottom product part circulation the first reboiler 4 of input in course of reaction (steam does thermal source)
Middle heated is boiled again, and re-enters in the first reaction tower 3 to provide heat；Another part tower bottom product input described first
Exchanged heat in heater 2 with the question response raw material from first condenser 1 to cool, while to from first condenser
1 question response raw material heating；And overhead product (the isobutene mixed gas obtained after the reaction) input first of the first reaction tower 3
Exchanged heat and cooled with the question response raw material in the first condenser 1 of input in condenser 1, while also treating reaction raw materials heating
Heating；Overhead product after cooling, which is inputted in first point of flow container 5, carries out gas-liquid separation, the top product (isobutyl of first point of flow container 5
Alkene gaseous mixture) exported through the first product output line 7, bottom product (concentration is about 35wt% t-butanol solution) input the
Carry out being heated to after 100 DEG C in two heaters 2 ', it is anti-through charging aperture input second with certain flow (such as 300kmol/hr)
Answer in tower 3 ', carry out tert-butyl alcohol dehydration reaction；Equally, tower bottom product part circulation the second reboiler of input in course of reaction
Heated and boiled again in 4 ' (steam does thermal source), and re-enter in the second reaction tower 3 ' to provide heat；Another part bottom of towe
Product is inputted in the secondary heater 2 ' and the material from the 4th conveying pipeline 12 is exchanged heat to cool, while
Charging to the second reaction tower 3 ' carries out heat temperature raising；And overhead product (the isobutene obtained after reaction of the second reaction tower 3 '
Mixed gas) cooled in the second condenser 1 ' of input, enters promoting the circulation of qi in overhead product second point of flow container 5 ' of input after cooling
Liquid is separated, and top product (isobutene gaseous mixture) is exported through the second product output line 7 ', and (concentration is about bottom product
50wt% t-butanol solution) re-enter in second reaction tower 3 ' that to carry out tert-butyl alcohol dehydration anti-through the 5th conveying pipeline 8
Should.
Paralleling model：
The first valve 91, the second valve 101 and the 3rd valve 111 are opened, the 4th valve 121 is closed, makes first module 01
It is connected in parallel with second unit 02, charging t-butanol solution (concentration is 94~98wt%) adds through the first condenser 1 input first
It is heated in hot device 2 after 100 DEG C, the first reaction tower 3 is inputted through charging aperture with certain flow (such as 300kmol/hr) respectively
In the second reaction tower 3 ', tert-butyl alcohol dehydration reaction is carried out；
In first reaction tower 3, (steam does heat to the first reboiler 4 of tower bottom product part circulation input in course of reaction
Source) middle heated is boiled again, and re-enter in the first reaction tower 3 to provide heat；The input of another part tower bottom product is described
Exchanged heat in primary heater 2 with the question response raw material from first condenser 1 to cool, while to cold from described first
The question response raw material heating of condenser 1；And overhead product (the isobutene mixed gas obtained after the reaction) input of the first reaction tower 3
First condenser 1 is exchanged heat to cool, while also the charging to the first reaction tower 3 is heated with question response raw material；Cooling
Overhead product afterwards inputs in first point of flow container 5 and carries out gas-liquid separation, the top product (isobutene gaseous mixture) of first point of flow container 5
Exported through the first product output line 7, bottom product (concentration is about 35wt% t-butanol solution) is through the 3rd conveying pipeline
11 re-enter progress tert-butyl alcohol dehydration reaction in first reaction tower 3；
Equally, in the second reaction tower 3 ', the second reboiler of tower bottom product part circulation input 4 ' in course of reaction (steams
Vapour does thermal source) middle heated is boiled again, and re-enter in the second reaction tower 3 ' to provide heat；Another part tower bottom product is defeated
Enter in the secondary heater 2 ' with the material from the 4th conveying pipeline 12 exchanged heat with cooling, while to from
The material of the 4th conveying pipeline 12 carries out heat temperature raising；And (what is obtained after reaction is different for the overhead product of the second reaction tower 3 '
Butylene mixed gas) cooled in the second condenser 1 ' of input, enters in overhead product second point of flow container 5 ' of input after cooling
Row gas-liquid separation, top product (isobutene gaseous mixture) is exported through the second product output line 7 ', and (concentration is about bottom product
35wt% t-butanol solution) re-enter in second reaction tower 3 ' that to carry out tert-butyl alcohol dehydration anti-through the 5th conveying pipeline 8
Should.
Under series model, when being carried out according to following reaction condition, the total conversion of the tert-butyl alcohol is not less than 98wt%.It is described
The reaction condition of series model is：The gating location of first reaction tower 3 and the second reaction tower 3 ' is the 25th piece of tower from the bottom to top
At plate, feed rate is 300kmol/hr, and bottom temperature is 150 DEG C；Tert-butyl alcohol concentration is in the charging of first reaction tower 3
97wt%；Tert-butyl alcohol concentration is 35wt% in the bottom product (i.e. the charging of the second reaction tower 3 ') of first point of flow container 5；First adds
The cold fluid pass outlet temperature of the hot fluid of hot device 2 and secondary heater 2 ' is 100 DEG C.
Under paralleling model, when being carried out according to following reaction condition, the total conversion of the tert-butyl alcohol is not less than 92wt%, and place
Reason ability is 2 times under series model.The reaction condition of the paralleling model is：First reaction tower 3 and the second reaction tower 3 '
Gating location is at the 25th block of column plate from the bottom to top, feed rate is 300kmol/hr, and bottom temperature is 150 DEG C, in charging
Tert-butyl alcohol concentration is 97wt%；The cold fluid pass outlet temperature of the hot fluid of primary heater 2 and secondary heater 2 ' is 100
℃。
Claims (5)
1. a kind of system for preparing isobutene for tert-butyl alcohol dehydration, it is characterised in that the system includes first module (01)
With second unit (02)；
The first module (01) includes the first condenser (1), primary heater (2), the first reaction tower (3), the first reboiler
And first point of flow container (5) (4)；The second unit (02) includes the second condenser (1 '), secondary heater (2 '), the second reaction
Tower (3 '), the second reboiler (4 ') and second point of flow container (5 ')；Wherein,
First condenser (1) is used to change the overhead product of first reaction tower (3) and the raw material tert-butyl alcohol of question response
Heat cooling；
The primary heater (2) is used to make the question response raw material heat absorption heating from first condenser (1)；Described first
The bottom of heater (2) is provided with the first conveying pipeline (9) and the second conveying pipeline (10), the first conveying pipeline (9) and set
There is the first valve (91), the first conveying pipeline (9) is used at least part question response will come from the primary heater (2)
Raw material sends into first reaction tower (3)；The second conveying pipeline (10) is provided with the second valve (101), and described second is defeated
Expects pipe line (10) is used at least part question response raw material from the primary heater (2) sending into second reaction tower
(3’)；
First reaction tower (3) is used to receive the question response raw material from the first conveying pipeline (9) and is taken off it
Water reaction prepares isobutene；
First reboiler (4) is used to make the tower bottom product heating of first reaction tower (3) to boil again；
First point of flow container (5) is used to receive the overhead product from first condenser (1) and gas-liquid point is carried out to it
From；The bottom of first point of flow container (5) is provided with the 3rd conveying pipeline (11) and the 4th conveying pipeline (12), and the described 3rd is defeated
Expects pipe line (11) is provided with the 3rd valve (111), and the 3rd conveying pipeline (11) is used for will be through first point of flow container (5) point
At least part liquid phase separated out delivers to first reaction tower (3) as overhead reflux；Set on the 4th conveying pipeline (12)
There is the 4th valve (121), the 4th conveying pipeline (12) is used at least part that will be isolated through first point of flow container (5)
Liquid phase delivers to the secondary heater (2 ')；
The secondary heater (2 ') is used to make the material heat absorption heating from the 4th conveying pipeline (12), to be heated up
Material；
Second reaction tower (3 ') is used to receive the heating material from the secondary heater (2 ') with coming from described second
The question response raw material of conveying pipeline (10), and its progress dehydration is prepared isobutene；
Second reboiler (4 ') is used to make the tower bottom product heating of second reaction tower (3 ') to boil again；
Second condenser (1 ') is used to receive the overhead product from second reaction tower (3 ') and it is condensed,
To obtain condensing material；
Second point of flow container (5 ') is used to carry out gas-liquid separation to the condensation material from second condenser (1 ')；It is described
The bottom of second point of flow container (5 ') is provided with the 5th conveying pipeline (8), for what will be isolated through second point of flow container (5 ')
At least part liquid phase is inputted in second reaction tower (3 ') as overhead reflux.
2. system according to claim 1, it is characterised in that the primary heater (2) is used to make to come from described first
The question response raw material of condenser (1) and the tower bottom product heat exchange of first reaction tower (3) heat up.
3. system according to claim 1, it is characterised in that the secondary heater (2 ') is used to make to come from the described 4th
The material of conveying pipeline (12) and the tower bottom product heat exchange of second reaction tower (3 ') heat up.
4. the system according to claim any one of 1-3, it is characterised in that first reaction tower (3) and described second
Reaction tower (3 ') includes column plate section and packing section from the bottom to top respectively, and the number of plates of the column plate section is 15-35, the filler
The filler number of plies of section is 2-8, and the charging aperture of first reaction tower (3) and second reaction tower (3 ') is arranged at from the tower
To the top of the packing section at the 1/2 of plate section.
5. system according to claim 4, it is characterised in that
The top exit of first point of flow container (5) is provided with the first product output line (7), for that will come from described first point
The top product output of flow container (5)；The top exit of second point of flow container (5 ') is provided with the second product output line (7 '),
For the top product from second point of flow container (5 ') to be exported.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720082568.1U CN206438057U (en) | 2017-01-18 | 2017-01-18 | The system that isobutene is prepared for tert-butyl alcohol dehydration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720082568.1U CN206438057U (en) | 2017-01-18 | 2017-01-18 | The system that isobutene is prepared for tert-butyl alcohol dehydration |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206438057U true CN206438057U (en) | 2017-08-25 |
Family
ID=59635408
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720082568.1U Active CN206438057U (en) | 2017-01-18 | 2017-01-18 | The system that isobutene is prepared for tert-butyl alcohol dehydration |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206438057U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112574008A (en) * | 2020-12-25 | 2021-03-30 | 南京晶典抗氧化技术研究院有限公司 | Method for synthesizing 2, 6 di-tert-butylphenol by using environment-friendly heterogeneous catalyst |
-
2017
- 2017-01-18 CN CN201720082568.1U patent/CN206438057U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112574008A (en) * | 2020-12-25 | 2021-03-30 | 南京晶典抗氧化技术研究院有限公司 | Method for synthesizing 2, 6 di-tert-butylphenol by using environment-friendly heterogeneous catalyst |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204932911U (en) | A kind of continuous rectification apparatus for maleic anhydride production | |
| CN207371131U (en) | A kind of reactive distillation process units | |
| CN206438057U (en) | The system that isobutene is prepared for tert-butyl alcohol dehydration | |
| CN109438251A (en) | A kind of methanol vapor phase catalytic ammoniation method prepares the method and device thereof of trimethylamine | |
| CN110918022A (en) | Temperature regulating system in methylamine synthesis | |
| CN109020824A (en) | A kind of formamide separation system and formamide separating technology | |
| CN101898930B (en) | Device for producing cyclohexane by adding hydrogen in benzene and synthesis process | |
| CN203829691U (en) | Liquid-gas linkage forced circulation hot pump low-temperature evaporation, concentration and crystallization device | |
| CN219209011U (en) | Nitroamine hydrogenation reaction thermal cycle recycling system | |
| CN103965001B (en) | Butylene oxidation-dehydrogenation reaction heat recovery method | |
| CN206069360U (en) | A kind of heat exchange of energy-conserving and environment-protective and condenser system | |
| CN205435021U (en) | System is used multipurposely to synthetic gas system ethylene glycol technology rectifying column overhead gas heat | |
| CN212166564U (en) | Chemical industry rectifier unit | |
| CN211514471U (en) | Temperature regulating system in methylamine synthesis | |
| CN210163383U (en) | Light hydrocarbon humidifying and steam distributing system | |
| CN204840984U (en) | Rectifying device | |
| CN209024426U (en) | A kind of material liquid preheating device in synthetic methylamine technique | |
| CN210314061U (en) | Rectification and purification device for synthesizing dimethyl oxalate by carbonylation of coal-made ethylene glycol | |
| CN111689827B (en) | Device and method for preparing styrene | |
| CN208933239U (en) | A kind of formamide separation system | |
| CN202671464U (en) | Urine concentration device used for urea production system | |
| CN201609598U (en) | Temperature control rectification column | |
| CN109824475A (en) | A method of utilizing the isobutene hydration production tert-butyl alcohol in mixing carbon four | |
| CN205740826U (en) | System for methanol synthesis | |
| CN205182686U (en) | Methyl alcohol system petrol reaction unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |