CN208562191U - The device of preparing tert-butanol by isobutene hydration - Google Patents
The device of preparing tert-butanol by isobutene hydration Download PDFInfo
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Abstract
The utility model relates to a kind of devices for preparing the tert-butyl alcohol, and in particular to a kind of device of preparing tert-butanol by isobutene hydration.Including three reactors, carbon four mixes hydrocarbon line and is connected to first reactor by first reactor feeding line, first reactor feeding line sets gradually the first distributor by feedstock direction, third distributor, circulating pump and First Heat Exchanger, the outlet at bottom of first reactor connects first reactor feeding line by first reactor circular route, desalination waterline is connected on first reactor circular route, the outlet at bottom of first reactor connects second reactor, the outlet at bottom of second reactor connects third reactor, the outlet at bottom of third reactor, which leads to, connects rectifying column, rectifier bottoms connection carbon four mixes hydrocarbon line, tert-butyl alcohol circular route is equipped with the tert-butyl alcohol and line is discharged.The utility model structure is simple, and it is poor to solve the problems, such as that carbon four mixes hydrocarbon property miscible with water, has the advantages that isobutene conversion is high, operational stability is good, low energy consumption, easy to industrialized production.
Description
Technical field
The utility model relates to a kind of devices for preparing the tert-butyl alcohol, and in particular to a kind of preparing tert-butanol by isobutene hydration
Device.
Background technique
The tert-butyl alcohol is a kind of important fine chemical product, currently, the universal method of the production tert-butyl alcohol is resin hydration method,
I.e. using sulfonic acid ion exchange resin as catalyst, hydrocarbon is mixed using the carbon four containing isobutene and produces the tert-butyl alcohol as raw water symphysis.Isobutyl
The hydro carbons such as alkene are low with the mutual solubility of water, when being mixed with liquid, two liquid phase easy to form.The key technology of isobutene hydration
It is that carbon four is made to mix hydrocarbon and water forms homogeneous dispersion or solution, the conversion ratio reacted with raising.On how to solve water hydrocarbon
The low problem of mutual solubility, existing related data are seen in report.
ZL00129128.9 uses the method for isobutene and water adverse current feeding into tower and the product tert-butyl alcohol continuously goes out tower
Mode of operation promotes reaction to carry out to positive direction to improve gas-liquid two-phase concentration difference, reaction balance limitation is broken through, to improve
Isobutene conversion, but this method there are water than big, air speed is small, shaping of catalyst is difficult the problems such as.ZL1511815A,
ZL101293813A improves the intersolubility of mixing carbon four and water using solvent or emulsifier, to improve reaction conversion ratio, above-mentioned skill
Art has the drawback that sewage containing emulsifier or solvent separation increase cost of investment and energy consumption.ZL98812676.1 is in order to increase
The intersolubility for adding hydration mixing carbon four, joined the tert-butyl alcohol in reaction raw materials, and the conversion ratio of reaction can achieve 80-90%,
The tert-butyl alcohol, water and liquid phase C_4 hydrocarbon three-phase are broken up dissolution by the effect of centrifugal pump by the technology, this is difficult to realize in practice.
ZL101124188A adds the tert-butyl alcohol as chaotropic agent in the feed, and in order to form homogeneous liquid phase, this technique improves in raw material
The content of the tert-butyl alcohol, but since isobutene hydration reaction is reversible reaction, the conversion ratio of isobutene is limited because of chemical balance,
In order to solve this problem, which adds rectifying column after each reactor, to remove tertiary butanol aqueous solution, in addition, each
Isobutene and water are added at reactor inlet, to promote reaction mobile to positive direction, the shortcomings that technology is that technique is cumbersome, investment
And energy consumption is higher.
Utility model content
In view of the deficiencies of the prior art, the purpose of the utility model is to provide a kind of dresses of preparing tert-butanol by isobutene hydration
It sets, structure is simple, and it is poor to solve the problems, such as that carbon four mixes hydrocarbon property miscible with water, has that isobutene conversion is high, operational stability is good, energy
Low advantage is consumed, it is easy to industrialized production.
The device of preparing tert-butanol by isobutene hydration described in the utility model, including three reactors, respectively first
Reactor, second reactor and third reactor, carbon four mix hydrocarbon line and are connected to first reactor by first reactor feeding line, the
One reactor feed line sets gradually the first distributor, third distributor, circulating pump and First Heat Exchanger by feedstock direction, and first
The outlet at bottom of reactor connects first reactor feeding line by first reactor circular route, connects on first reactor circular route
Desalination waterline is connect, the outlet at bottom of first reactor also passes through second reactor feeding line connection second reactor, the second reaction
The outlet at bottom of device connects third reactor by third reactor feed line, and the outlet at bottom of third reactor passes through rectifying column
Feeding line connects rectifying column, and reboiler is arranged in rectifying column lower part, and rectifier bottoms are arranged kettle material and produce line, kettle material
Extraction line connects carbon four by tert-butyl alcohol circular route and mixes hydrocarbon line, and tert-butyl alcohol circular route is equipped with the tert-butyl alcohol and line is discharged.
Wherein:
The inner lower of first reactor is equipped with cooling water line.
Between the first distributor and third distributor, first reactor circular route is equipped with first reactor circular route
Second distributor, the second distributor is between first reactor feeding line and desalination waterline.
Second reactor feeding line is equipped with the second heat exchanger, and third reactor feed line is equipped with third heat exchanger, essence
Tower feeding line is evaporated equipped with tower bottom of rectifying tower heat exchanger.
Line is distillated by tower top at the top of rectifying column and connects return tank import, tower top distillates line equipped with overhead condenser, returns
The outlet of stream tank is separately connected return wire by pipeline and carbon four produces line.
Kettle material extraction line connects carbon four by tert-butyl alcohol circular route and mixes hydrocarbon line are as follows: kettle material produces line and is equipped with tower
Kettle material extraction pump, kettle material produce line and connect the import of tower bottom of rectifying tower heat exchanger, and tower bottom of rectifying tower heat exchanger exit passes through
Pipeline connects the tert-butyl alcohol and line is discharged, and tower bottom of rectifying tower heat exchanger exit connects carbon four by tert-butyl alcohol circular route and mixes hydrocarbon line, tertiary fourth
Alcohol circular route is equipped with tert-butyl alcohol cooler.
Downspout and 50-60 block tower tray are equipped in rectifying column, tower tray uses composite holes miniature valve high-efficient tower plate, and downspout is adopted
Downspout is tilted with more flangings.Rectifying column feeding temperature is 80-90 DEG C, and tower top temperature is 50-80 DEG C, column bottom temperature 120-
150 DEG C, pressure tower 0.3-0.7MPa.
The utility model is provided with 3 reactors, adds heat exchanger at each reactor inlet；Preferably, the first reaction
The feeding temperature of device, second reactor and third reactor is between 40-60 DEG C, and first reactor feeding temperature is than second
Reactor feed temperature is 1-10 DEG C high, and second reactor feeding temperature is 1-10 DEG C higher than third reactor feed temperature, and first is anti-
The pressure for answering device, second reactor and third reactor is 0.8-0.9Mpa.
First reactor, second reactor and third reactor are fixed bed reactors, first reactor, the second reaction
The catalyst bed ratio of height to diameter of device and third reactor is 0.8-1.1, and the catalyst of filling is large aperture strong-acid type cation
Exchanger resin, the Catalyst packing volume ratio of first reactor, second reactor and third reactor are 1:0.5-0.9:0.2-
0.5。
First reactor entrance desalted water and carbon four mix hydrocarbon, first reactor recycle stock and the tertiary fourth of rectifying tower bottoming cycle
The mass ratio of alcohol is 1:5-6:18-20:4-6, and it is 0.8-1.5h that carbon four, which mixes the volume space velocity of hydrocarbon, in first reactor charging-1；Carbon
Four mixed hydrocarbon are that the carbon four that isobutene content is 40-50wt.% mixes hydrocarbon；It is liquid that carbon four, which mixes the carbon four in hydrocarbon line and mixes hydrocarbon, and temperature is
20-40 DEG C, the tert-butyl alcohol temperature in tert-butyl alcohol circular route is 20-40 DEG C.
Material is after three reactors, and water alcohol mass ratio drops to 1:6 in material, reaction motive force have already decreased to compared with
Low-level can obtain the tert-butyl alcohol that concentration is 85wt% or more after material decarburization four.
The utility model circulating pump, reflux pump, kettle material extraction pump are using centrifugal pump, First Heat Exchanger, second
Heat exchanger, third heat exchanger, tower bottom of rectifying tower heat exchanger, overhead condenser, reboiler, tert-butyl alcohol cooler are using floating head
One or more of formula heat exchanger, fixed tube-sheet exchanger, U-shaped curved formula heat exchanger.
Using the preparation process of the device of preparing tert-butanol by isobutene hydration described in the utility model, steps are as follows:
The carbon four for mixing hydrocarbon line from carbon four mixes hydrocarbon and mixes with the tert-butyl alcohol from tert-butyl alcohol circular route through the first distributor, comes
It is mixed in the second distributor from the desalted water of desalted water line with the material from first reactor circular route, above-mentioned two strands of materials
It is mixed in third distributor.Mixed material through circulating pump pressurize, First Heat Exchanger heat exchange after along first reactor into
Stockline enters first reactor, and under the effect of the catalyst, carbon four mixes the part isobutene in hydrocarbon and reacts generation uncle with desalted water
Butanol, reaction product part enter first reactor circular route as recycle stock and return to the second distributor, and another part passes through
After second heat exchanger is cooling, enter second reactor reaction along second reactor feeding line, reaction product exchanges heat by third
After device is cooling, enter third reactor reaction along third reactor feed line, reaction product passes through tower bottom of rectifying tower heat exchanger
After heating, enter rectifying column along rectifying column feeding line.Material gas-liquid under the action of the thermal drivers of reboiler and phegma
Two phase countercurrent flow contact carries out fraction cutting, and overhead C_4 hydrocarbon along tower top distillates line, and successively to pass through overhead condenser cold
After solidifying, reflux pump pressurization, a part returns to rectifying column along return wire as phegma, and a part produces outside line along carbon four
Row, the tower bottom tert-butyl alcohol produce line after the pressurization of kettle material extraction pump, tower bottom of rectifying tower heat exchanger are cooling along kettle material,
A part returns to the first distributor along tert-butyl alcohol circular route, and line outlet is discharged along the tert-butyl alcohol in a part.
Compared with prior art, the utility model has the advantage that
(1) currently, in the existing production process for mixing the hydrocarbon hydration production tert-butyl alcohol using the tert-butyl alcohol as solvent, carbon four, i.e.,
Make to be that reaction begins with a large amount of tert-butyl alcohols presence, mixes carbon four and the intersolubility of water is still poor, be embodied in reactor and enter
Sampling analysis poor repeatability at mouthful.The utility model carbon four mixes hydrocarbon and first mixes with the circulation tert-butyl alcohol in the first distributor, desalted water
It is mixed with first reactor recycle stock, last two strands of materials are mixed in third distributor, are had the advantage that and are added distributor
To increase the contact area of fluid；Using solubility of the isobutene in tertiary butanol aqueous solution with the increase of tert-butyl alcohol concentration and
Carbon four is mixed hydrocarbon and mixed in the first distributor with the high concentration tert-butyl alcohol aqueous solution at rectifying column bottom, makes carbon four by the characteristics of increase
Mixed hydrocarbon and high concentration tert-butyl alcohol aqueous solution are formed homogeneously, and first reactor recycle stock it is very easy formed with desalted water it is another
Stock homogeneous phase solution, this two bursts equal phase materials polarity are similar, and surface tension very little, the mixed process in third distributor is one
Diffusion of components process, alternate resistance very little.The advantages of above-mentioned design is the intersolubility for improving carbon four and mixing hydrocarbon and water.
(2) the utility model is provided with 3 reactors, heat exchanger is added at each reactor inlet, and in the first reaction
Cooling water line is arranged in middle and lower part in device, so that entirely reaction is maintained lower temperature levels, can effectively avoid because bed temperature is excessively high
Caused by catalyst sulfonate ion fall off and the problems such as isobutene polymerisation, be also beneficial to the progress of hydration reaction.
(3) the Catalyst packing volume of first reactor, second reactor and third reactor successively reduces, and can effectively subtract
The isobutene residence time in few subsequent reactor, reduce the production quantity of the by-products such as isobutene dimer, sec-butyl alcohol.
Detailed description of the invention
Fig. 1 is the apparatus structure schematic diagram of the utility model embodiment preparing tert-butanol by isobutene hydration；
In figure: 1, carbon four mixes hydrocarbon line；2, the first distributor；3, desalination waterline；4, the second distributor；5, third distributor；
6, first reactor feeding line；7, First Heat Exchanger；8, first reactor；9, circulating pump；10, first reactor circular route；11,
Second reactor feeding line；12, the second heat exchanger；13, second reactor；14, third reactor feed line；15, third exchanges heat
Device；16, third reactor；17, tower bottom of rectifying tower heat exchanger；18, rectifying column feeding line；19, rectifying column；20, overhead condensation
Device；21, tower top distillates line；22, return tank；23, reflux pump；24, return wire；25, carbon four produces line；26, reboiler；27, tower
Kettle material produces line；28, kettle material extraction pump；29, line is discharged in the tert-butyl alcohol；30, tert-butyl alcohol circular route；31, the tert-butyl alcohol is cooling
Device, 32, cooling water line.
Specific embodiment
The utility model is described further below with reference to embodiment.
Embodiment 1
A kind of device of preparing tert-butanol by isobutene hydration, as shown in Figure 1, including three reactors, respectively first is anti-
Device 8, second reactor 13 and third reactor 16 are answered, carbon four mixes hydrocarbon line 1 and passes through first reaction of the connection of first reactor feeding line 6
Device 8, first reactor feeding line 6 set gradually the first distributor 2, third distributor 5, circulating pump 9 and first by feedstock direction
Heat exchanger 7, the outlet at bottom of first reactor 8 connect first reactor feeding line 6 by first reactor circular route 10, and first
Desalination waterline 3 is connected on reactor cycles line 10, the outlet at bottom of first reactor 8 also passes through the company of second reactor feeding line 11
Second reactor 13 is connect, the outlet at bottom of second reactor 13 connects third reactor 16 by third reactor feed line 14,
The outlet at bottom of third reactor 16 connects rectifying column 19 by rectifying column feeding line 18, and reboiler is arranged in 19 lower part of rectifying column
26,19 bottom of rectifying column is arranged kettle material and produces line 27, and kettle material produces line 27 and connects carbon by tert-butyl alcohol circular route 30
Four mixed hydrocarbon lines 1, tert-butyl alcohol circular route 30 are equipped with the tert-butyl alcohol and line 29 are discharged.
The inner lower of first reactor 8 is equipped with cooling water line 32.
First reactor circular route 10 is between the first distributor 2 and third distributor 5, first reactor circular route 10
It is equipped with the second distributor 4, the second distributor 4 is between first reactor feeding line 6 and desalination waterline 3.
Second reactor feeding line 11 is equipped with the second heat exchanger 12, and third reactor feed line 14 exchanges heat equipped with third
Device 15, rectifying column feeding line 18 are equipped with tower bottom of rectifying tower heat exchanger 17.
Line 21 is distillated by tower top at the top of rectifying column 19 and connects 22 import of return tank, it is cold equipped with tower top that tower top distillates line 21
Condenser 20, the outlet of return tank 22 is separately connected return wire 24 by pipeline and carbon four produces line 25.
Kettle material extraction line 27 connects carbon four by tert-butyl alcohol circular route 30 and mixes hydrocarbon line 1 are as follows: kettle material produces line 27
It is equipped with kettle material extraction pump 28, kettle material produces line 27 and connects 17 import of tower bottom of rectifying tower heat exchanger, tower bottom of rectifying tower
The outlet of heat exchanger 17 connects the tert-butyl alcohol by pipeline and line 29 is discharged, and the outlet of tower bottom of rectifying tower heat exchanger 17 passes through tert-butyl alcohol circular route
30 connection carbon four mix hydrocarbon line 1, and tert-butyl alcohol circular route 30 is equipped with tert-butyl alcohol cooler 31.
Downspout and 50-60 block tower tray are equipped in rectifying column 19, tower tray uses composite holes miniature valve high-efficient tower plate, downspout
Downspout is tilted using more flangings.
Using the preparation process of the device of the preparing tert-butanol by isobutene hydration, steps are as follows:
It is mixed through the first distributor 2 that the carbon four for mixing hydrocarbon line 1 from carbon four mixes hydrocarbon and the tert-butyl alcohol from tert-butyl alcohol circular route 30
It closing, the desalted water from desalination waterline 3 mixes in the second distributor 4 with the material from first reactor circular route 10, on
Two strands of materials are stated to mix in third distributor 5.Mixed material through circulating pump 9 pressurize, First Heat Exchanger 7 exchange heat after along
First reactor feeding line 6 enters first reactor 8, and under the effect of the catalyst, carbon four mixes the part isobutene in hydrocarbon and takes off
Salt water reaction generates the tert-butyl alcohol, and reaction product part enters first reactor circular route 10 as recycle stock and returns to the second distribution
Device 4, it is anti-that another part enters second reactor 13 after the second heat exchanger 12 is cooling, along second reactor feeding line 11
It answers, reaction product enters third reactor 16 along third reactor feed line 14 and reacts after third heat exchanger 15 is cooling,
Reaction product enters rectifying column 19 after the heating of tower bottom of rectifying tower heat exchanger 17, along rectifying column feeding line 18.Material is again
Gas-liquid two-phase counter current contacting carries out fraction cutting, overhead C_4 hydrocarbon under the action of boiling the thermal drivers and phegma of device 26
Along tower top distillate line 21 successively by overhead condenser 20 condensation, reflux pump 23 pressurize after, a part as phegma along
Return wire 24 returns to rectifying column 19, and a part produces 25 outlet of line along carbon four, and the tower bottom tert-butyl alcohol produces line along kettle material
27 after 28 pressurization of kettle material extraction pump, tower bottom of rectifying tower heat exchanger 17 are cooling, and a part is along tert-butyl alcohol circular route 30
The first distributor 2 is returned to, 29 outlet of line is discharged along the tert-butyl alcohol in a part.
1 feed carbon four of embodiment mixes hydrocarbon composition as shown in table 1, and it is 20 DEG C that carbon four, which mixes hydrocarbon temperature,.Recycling tert-butyl alcohol temperature is
20 DEG C, the content for recycling the tert-butyl alcohol in the tert-butyl alcohol is 89wt.%.Desalted water, the carbon four of 8 entrance of first reactor mix hydrocarbon, come from
The mass ratio of the material of first reactor circular route 10 and the tert-butyl alcohol from tert-butyl alcohol circular route 30 is 1:6:18:4.
Table 1
| Component | Isobutene | Iso-butane |
| Content (wt.%) | 48 | 52 |
The catalyst bed ratio of height to diameter of first reactor 8, second reactor 13 and third reactor 16 is 0.8, and first is anti-
The Catalyst packing volume ratio for answering device 8, second reactor 13 and third reactor 16 is 1:0.9:0.5.
It is 1.0h that carbon four, which mixes the volume space velocity of hydrocarbon, in the charging of first reactor 8-1, feeding temperature is 55 DEG C, and reaction pressure is
0.9MPa, outlet temperature are 60 DEG C；13 feeding temperature of second reactor is 49 DEG C, reaction pressure 0.87MPa, and outlet temperature is
53℃；16 feeding temperature of third reactor is 40 DEG C, reaction pressure 0.86MPa, and outlet temperature is 43 DEG C.After reaction, isobutyl
Alkene total conversion 87%.
Downspout and 50 pieces of tower trays are equipped in rectifying column 19, tower tray uses composite holes miniature valve high-efficient tower plate, and downspout is adopted
Downspout is tilted with more flangings, feeding temperature is 80 DEG C, and tower top temperature is 50 DEG C, and column bottom temperature is 120 DEG C, and pressure tower is
0.5MPa。
Tower bottom of rectifying tower effluent tert-butyl alcohol concentration is 89wt.%, and Diisobutylene concentration is 0.01wt.%, sec-butyl alcohol
Concentration is 0.01wt.%.
Embodiment 2
The device for the preparing tert-butanol by isobutene hydration that embodiment 2 uses is same as Example 1, and difference is:
Feed carbon four mixes hydrocarbon composition as shown in table 2, and it is 40 DEG C that carbon four, which mixes hydrocarbon temperature,.Recycling tert-butyl alcohol temperature is 40 DEG C, is followed
The content of the tert-butyl alcohol is 85wt.% in the ring tert-butyl alcohol.Desalted water, the carbon four of 8 entrance of first reactor mix hydrocarbon, from the first reaction
The mass ratio of the material of device circular route 10 and the tert-butyl alcohol from tert-butyl alcohol circular route 30 is 1:5:20:6.
Table 2
| Component | Isobutene | Iso-butane |
| Content (wt.%) | 40 | 60 |
The catalyst bed ratio of height to diameter of first reactor 8, second reactor 13 and third reactor 16 is 1.0, and first is anti-
The Catalyst packing volume ratio for answering device 8, second reactor 13 and third reactor 16 is 1:0.6:0.3.
It is 0.8h-1 that carbon four, which mixes the volume space velocity of hydrocarbon, in the charging of first reactor 8, and feeding temperature is 50 DEG C, and reaction pressure is
0.9MPa, outlet temperature are 55 DEG C；13 feeding temperature of second reactor is 49 DEG C, reaction pressure 0.87MPa, and outlet temperature is
53℃；16 feeding temperature of third reactor is 43 DEG C, reaction pressure 0.86MPa, and outlet temperature is 46 DEG C.After reaction, isobutyl
Alkene total conversion 85%.Downspout and 55 pieces of tower trays are equipped in rectifying column 19, tower tray uses composite holes miniature valve high-efficient tower plate, drop
Liquid pipe tilts downspout using more flangings.Feeding temperature is 90 DEG C, and tower top temperature is 75 DEG C, and column bottom temperature is 130 DEG C, pressure tower
For 0.6Mpa.
Tower bottom of rectifying tower effluent tert-butyl alcohol concentration is 85wt.%, and Diisobutylene concentration is 0.01wt.%, sec-butyl alcohol
Concentration is 0.01wt.%.
Claims (7)
1. a kind of device of preparing tert-butanol by isobutene hydration, it is characterised in that: including three reactors, the respectively first reaction
Device (8), second reactor (13) and third reactor (16), carbon four mix hydrocarbon line (1) and are connected to by first reactor feeding line (6)
First reactor (8), first reactor feeding line (6) set gradually the first distributor (2), third distributor by feedstock direction
(5), the outlet at bottom of circulating pump (9) and First Heat Exchanger (7), first reactor (8) passes through first reactor circular route (10)
It connects first reactor feeding line (6), connects desalination waterline (3) on first reactor circular route (10), first reactor (8)
Outlet at bottom also passes through second reactor feeding line (11) connection second reactor (13), the outlet at bottom of second reactor (13)
Third reactor (16) are connected by third reactor feed line (14), the outlet at bottom of third reactor (16) passes through rectifying column
Feeding line (18) connects rectifying column (19), and reboiler (26) are arranged in rectifying column (19) lower part, and tower is arranged in rectifying column (19) bottom
Kettle material produces line (27), and kettle material extraction line (27) connects carbon four by tert-butyl alcohol circular route (30) and mixes hydrocarbon line (1), tertiary fourth
Alcohol circular route (30) is equipped with tert-butyl alcohol discharge line (29).
2. the device of preparing tert-butanol by isobutene hydration according to claim 1, it is characterised in that: first reactor (8)
Inner lower be equipped with cooling water line (32).
3. the device of preparing tert-butanol by isobutene hydration according to claim 1, it is characterised in that: first reactor circulation
For line (10) between the first distributor (2) and third distributor (5), first reactor circular route (10) is equipped with the second distribution
Device (4), the second distributor (4) are located between first reactor feeding line (6) and desalination waterline (3).
4. the device of preparing tert-butanol by isobutene hydration according to claim 1, it is characterised in that: second reactor charging
Line (11) be equipped with the second heat exchanger (12), third reactor feed line (14) be equipped with third heat exchanger (15), rectifying column into
Expects pipe line (18) is equipped with tower bottom of rectifying tower heat exchanger (17).
5. the device of preparing tert-butanol by isobutene hydration according to claim 1, it is characterised in that: at the top of rectifying column (19)
Line (21) are distillated by tower top and connect return tank (22) import, and tower top distillates line (21) equipped with overhead condenser (20), reflux
Tank (22) outlet is separately connected return wire (24) by pipeline and carbon four produces line (25).
6. the device of preparing tert-butanol by isobutene hydration according to claim 1, it is characterised in that: kettle material produces line
(27) carbon four is connected by tert-butyl alcohol circular route (30) and mix hydrocarbon line (1) are as follows: kettle material produces line (27) and is equipped with kettle material
Extraction pump (28), kettle material produce line (27) and connect tower bottom of rectifying tower heat exchanger (17) import, tower bottom of rectifying tower heat exchanger
(17) outlet connects tert-butyl alcohol discharge line (29) by pipeline, and tower bottom of rectifying tower heat exchanger (17) outlet passes through tert-butyl alcohol circular route
(30) connection carbon four mixes hydrocarbon line (1), and tert-butyl alcohol circular route (30) is equipped with tert-butyl alcohol cooler (31).
7. the device of preparing tert-butanol by isobutene hydration according to claim 1, it is characterised in that: set in rectifying column (19)
There are downspout and 50-60 block tower tray, tower tray uses composite holes miniature valve high-efficient tower plate, and downspout tilts descending liquid using more flangings
Pipe.
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| CN201821112347.5U CN208562191U (en) | 2018-07-13 | 2018-07-13 | The device of preparing tert-butanol by isobutene hydration |
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| CN201821112347.5U CN208562191U (en) | 2018-07-13 | 2018-07-13 | The device of preparing tert-butanol by isobutene hydration |
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