CN207877621U - A kind of device that octyl alconyl raffinate recycles - Google Patents
A kind of device that octyl alconyl raffinate recycles Download PDFInfo
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- CN207877621U CN207877621U CN201820122685.0U CN201820122685U CN207877621U CN 207877621 U CN207877621 U CN 207877621U CN 201820122685 U CN201820122685 U CN 201820122685U CN 207877621 U CN207877621 U CN 207877621U
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Abstract
The utility model is related to the devices that a kind of octyl alconyl raffinate recycles, including the miscellaneous oily tower of sequentially connected raw material pans, weight-removing column, reactor, knockout drum, dehydrating tower, butanol tower, falling film evaporator, gas-liquid separator, C5~C8 and octanol tower.It first carries out taking off before octyl alconyl raffinate hydrogenation reaction in the utility model handling again, enter reactor after de- weight, react with hydrogen completion plus hydrogen under the action of catalyst, reaction temperature is 60~160 DEG C, reaction pressure is 2~5MPa, add after hydrogen octyl alconyl raffinate to enter distillation system and isolate the products such as the miscellaneous oil of butanol, octanol, C5~C8, heavy component, wherein butanol, octanol products purity can meet customer need up to 99% or more.
Description
Technical field
The utility model is related to octyl alconyl utilization technology field, particularly relate to what a kind of octyl alconyl raffinate recycled
Device.
Background technology
Butanol and octanol are important fine chemical material, and purposes is very extensive, and main is for producing plasticizer
Dioctyl phthalate and neck dibatyl phithalate.With the development of China's plastics industry, need of the market to butanol, octanol
The amount of asking cumulative year after year.Oxo synthesis produces in the device of octyl alconyl, and discharge 10% per hour contains butyraldehyde, butanol, octanol
And the material composition of polymer etc., it is commonly called as octyl alconyl raffinate.Original designs these raffinates and is sold as fuel, and value is very low, makes
At waste, it is contour attached to obtain butyraldehyde, butanol, octanol due to containing a large amount of useful substances in octyl alconyl raffinate, after purification ＆ isolation
Value added material can turn waste into wealth, and create considerable economic benefit.
Utility model content
In view of this, the main purpose of the utility model is to provide the devices that a kind of octyl alconyl raffinate recycles.
In order to achieve the above object, the technical solution of the utility model is realized in：
The device that a kind of octyl alconyl raffinate recycles, including sequentially connected raw material pans, weight-removing column, reactor,
The miscellaneous oily tower of knockout drum, dehydrating tower, butanol tower, falling film evaporator, gas-liquid separator, C5~C8 and octanol tower.
As further preferred technical solution, wherein the raw material pans are exported equipped with raw material pans, it is described
It is respectively equipped with weight-removing column material inlet, weight-removing column kettle extraction mouth and weight-removing column top extraction mouth on weight-removing column, divides on the reactor
It She You not reactor fluid inlet, the import of reactor gas phase, reactor liquid-phase outlet and reactor gaseous phase outlet；The gas-liquid point
From being respectively equipped with the import of knockout drum gas phase, knockout drum fluid inlet, knockout drum liquid-phase outlet and gas-liquid on tank
Knockout drum gaseous phase outlet；Dehydrating tower import, dehydration overhead extraction mouth and dehydrating tower kettle extraction mouth are respectively equipped on the dehydrating tower；
Butanol tower feed inlet, butanol overhead extraction mouth and butanol tower reactor extraction mouth are respectively equipped on the butanol tower；The falling film evaporation
Falling film evaporator entrance and falling film evaporator outlet are respectively equipped on device；Be respectively equipped on the gas-liquid separator gas-liquid divide device into
Mouth, gas-liquid separator gaseous phase outlet and gas-liquid separator liquid-phase outlet；It is miscellaneous it to be respectively equipped with C5~C8 on the miscellaneous oily towers of the C5~C8
The miscellaneous oily overhead extraction mouth of oily tower feed inlet, C5~C8 and the miscellaneous oily tower reactors of C5~C8 produce mouth；It is respectively equipped on the octanol tower pungent
Alcohol tower feed inlet, octanol overhead extraction mouth and octanol tower reactor produce mouth.
As further preferred technical solution, wherein the upper end of the reactor is equipped with reactor gas phase import；It is described
The upper end of knockout drum is equipped with knockout drum gas phase import；The upper end of the dehydrating tower is equipped with dehydration overhead extraction mouth, institute
It states dehydration overhead extraction mouth by pipeline to be connected with oil-water decanter, oil-water decanter object is respectively equipped on the oil-water decanter
Material extraction mouth and oil-water decanter waste water produce mouth；The upper end of the butanol tower is equipped with butanol overhead extraction mouth；C5~the C8
The upper end of miscellaneous oil tower is equipped with the miscellaneous oily overhead extraction mouths of C5~C8；The upper end of the octanol tower is equipped with octanol overhead extraction mouth.
As further preferred technical solution, wherein the lower end of the raw material pans is exported equipped with raw material pans,
The outlet of raw material pans is by pipeline via after the first raw material heat exchanger, the second raw material heat exchanger, feed preheater and set on institute
The weight-removing column material inlet for stating weight-removing column side is connected；The upper end of the weight-removing column is equipped with weight-removing column top and produces mouth, weight-removing column top
Extraction mouth is connected with the reactor fluid inlet set on reactor top side by pipeline；The other side of the reactor
Equipped with reactor gaseous phase outlet, reactor gaseous phase outlet and the knockout drum gas phase import for being set to the knockout drum side
It is connected by pipeline, the lower end of the reactor is equipped with reactor liquid-phase outlet, the side of reactor liquid-phase outlet and set on institute
The knockout drum fluid inlet for stating knockout drum side is connected by pipeline, and the other side is changed by pipeline via the first raw material
Hot device, recycle stock heat exchanger are connected with Reactor inlet；The lower end of the knockout drum goes out equipped with knockout drum liquid phase
Mouthful, knockout drum liquid-phase outlet is connected by pipeline with the dehydrating tower material inlet set on the dehydrating tower side；It is described de-
The lower part other side of water tower is equipped with dehydrating tower tower reactor and produces mouth, and dehydrating tower tower reactor produces mouth by pipeline and is set to the butanol tower
The butanol tower material inlet of side is connected, and the lower part other side of the butanol tower is equipped with butanol tower reactor and produces mouth, and butanol tower reactor is adopted
Outlet is connected by pipeline with the falling film evaporator material inlet set on the falling film evaporator upper end, the falling film evaporator
Lower end is equipped with falling film evaporator material outlet, and falling film evaporator material outlet is by pipeline and is set to the gas-liquid separator side
Gas-liquid separator material inlet be connected, the upper end of the gas-liquid separator is equipped with gas-liquid separator gaseous phase outlet, gas-liquid separation
Device gaseous phase outlet is connected by pipeline with C5~C8 tower material inlets set on the miscellaneous sides You Ta the C5~C8, and the C5~
The lower part other side of the miscellaneous oily towers of C8 is equipped with C5~C8 tower tower reactors and produces mouth, and C5~C8 tower tower reactors produce mouth by pipeline and are set to institute
The octanol tower material inlet for stating octanol tower side is connected, and the lower part side of the octanol tower is equipped with octanol tower reactor and produces mouth, octanol
Tower reactor produces mouth, the knockout drum liquid-phase outlet set on the gas-liquid separator lower end, taking off set on the weight-removing column lower end
Weight tower reactor produces mouth and removes heavy constituent tank after the second raw material heat exchanger together by the way that pipeline is connected.
As further preferred technical solution, wherein the reactor is liquid phase hydrogenation reactor；The weight-removing column, fourth
The miscellaneous oily tower of alcohol tower, C5~C8, octanol tower are negative pressure tower, and the charging of the miscellaneous oily towers of the C5~C8 is gas phase.
As further preferred technical solution, wherein the octyl alconyl raffinate hydrogenation reaction master equation in the reactor
For：
As further preferred technical solution, wherein the catalyst is carbon-based nickel-alumina catalyst.
Aldehyde hydrogen addition technology has two kinds of liquid-phase hydrogenatin and gas phase hydrogenation, all more mature, in the technical program, due to octyl alconyl
Raffinate component feature (material boiling point is higher, only needs partial hydrogenation), adds hydrogen mode to select liquid-phase hydrogenatin.Liquid-phase hydrogenatin converts more
Completely, it is not necessarily to the cycle of the vaporization and hydrogen of material, energy consumption is relatively low, and flow is shorter.The reaction of liquid-phase hydrogenatin simultaneously is more violent, residual
A large amount of inert fractions make reaction become more to mitigate in liquid.
Hydrogenation catalyst selects carbon-based nickel-alumina catalyst, to avoid heavy component in raffinate from having an impact the service life of catalyst,
First material take off before hydrogenation reaction and be handled again.Octyl alconyl raffinate enters liquid phase hydrogenation reactor after de- weight, makees in catalyst
Complete to add hydrogen with lower react with hydrogen, reaction temperature is 60~160 DEG C, and reaction pressure is 2~5MPa.Add octyl alconyl after hydrogen
Raffinate enters distillation system and isolates the products such as the miscellaneous oil of butanol, octanol, C5~C8, heavy component, wherein butanol, octanol products purity
Up to 99% or more, can meet customer need.
The utility model has following advantageous effects：Carbon-based nickel-alumina catalyst is selected, to the fourth in octyl alconyl raffinate
The materials such as aldehyde, octenal carry out plus hydrogen, improve added value of product；Repeated hydrogenation after taking off again is carried out to octyl alconyl raw material, is stripped of
The long-chain component in blocking catalyst duct extends the service life of catalyst；Octyl alconyl raffinate raw material first passes through the first raw material
Heat exchanger, the second raw material heat exchanger pass through feed preheater again after successively carrying out heat exchange heating with reaction cycle material, heavy component
Into weight-removing column, step recycling is carried out to waste heat in system, has reduced production cost；Object after reaction system partial reaction
Material is recycled, and is participated in reacting with the latter same reactor that enters of raw material mixing, by the flow and temperature of control loop material, be risen
The effect for adjusting reaction feed component and temperature has been arrived, to play the role of controlling hydrogenation reaction rate and reaction heat, has been carried
The controllability of high hydrogenation reaction and safety；Dehydrating tower using the materials such as butanol, trimethylheptane and water its boilings characteristic from
Tower top is dehydrated, then is detached water with these materials by gun barrel, material can in can return containing a large amount of butanol
Octyl alconyl raw material pans are returned, the waste of active ingredient is avoided；Weight-removing column, butanol tower, C5~C8 towers, octanol tower are grasped for negative pressure
Make, material caused by avoiding high temperature decomposes, while greatly reducing the energy consumption of distillation operation；After adding hydrogen, rectifying, device
The products such as the miscellaneous oil of output butanol, octanol, C5~C8, C12-C16 heavy components, wherein butanol, octanol products purity up to 99% with
On, it can meet customer need.
Description of the drawings
Fig. 1 is the overall structure diagram of the utility model.
Wherein, 1- raw materials pans；11- raw material pans export；12- the second raw material heat exchangers；13- feed preheaters；
2- weight-removing columns；21- weight-removing column material inlets；22- weight-removing column kettles produce mouth；23- weight-removing columns top produces mouth；3- reactors；31- is anti-
Answer device fluid inlet；32- reactor gas phase imports；33- reactor liquid-phase outlets；34- the first raw material heat exchangers；35- recycles
Expect heat exchanger；36- reactor gaseous phase outlets；4- knockout drums；41- knockout drum gas phase imports；42- knockout drums
Fluid inlet；43- knockout drum liquid-phase outlets；44- knockout drum gaseous phase outlets；5- dehydrating towers；51- dehydrating tower imports；
52- is dehydrated overhead extraction mouth；53- oil-water decanters；54- oil-water decanter materials produce mouth；55- oil-water decanter waste water produces
Mouthful；56- dehydrating tower kettles produce mouth；6- butanol towers；61- butanol tower feed inlets；62- butanol overhead extraction mouths；63- butanol tower reactors are adopted
Outlet；7- falling film evaporators；71- falling film evaporator entrances；72- falling film evaporators export；8- gas-liquid separators；81- gas-liquids point
Device import；82- gas-liquid separator gaseous phase outlets；83- gas-liquid separator liquid-phase outlets；The miscellaneous oily towers of 9-C5~C8；91-C5~C8 is miscellaneous
Oily tower feed inlet；The miscellaneous oily overhead extraction mouths of 92-C5~C8；93-C5~C8 is miscellaneous, and oily tower reactor produces mouth；10- octanol towers；101- is pungent
Alcohol tower feed inlet；102- octanol overhead extraction mouths；103- octanol tower reactors produce mouth.
Specific implementation mode
The utility model is described in further detail with specific implementation case below in conjunction with the accompanying drawings, but lifted case study on implementation is not made
For the restriction to the utility model.
It will be readily understood by those skilled in the art that Fig. 1 is simplification figure, a commercial plants may need more to set
It is standby, such as pump, vacuum pump, compressor, reboiler, return tank, tower top cooler, temperature sensor, pressure sensor, flowmeter,
Regulating valve etc..These equipment are consistent with common engineering practice, are no longer described in detail.
As shown in Figure 1, the utility model is related to the device that a kind of octyl alconyl raffinate recycles, including sequentially connected original
Expect pans 1, weight-removing column 2, reactor 3, knockout drum 4, dehydrating tower 5, butanol tower 6, falling film evaporator 7, gas-liquid separator
8, the miscellaneous oily towers 9 of C5~C8 and octanol tower 10.
The raw material pans 1 are equipped with raw material pans and export 11, and weight-removing column material is respectively equipped on the weight-removing column 2
Import 21, weight-removing column kettle extraction mouth 22 and weight-removing column top produce mouth 23, and reactor fluid inlet is respectively equipped on the reactor 3
31, reactor gas phase import 32, reactor liquid-phase outlet 33 and reactor gaseous phase outlet 36；On the knockout drum 4 respectively
Equipped with knockout drum gas phase import 41, knockout drum fluid inlet 42, knockout drum liquid-phase outlet 43 and gas-liquid separation
Tank gaseous phase outlet 44；Dehydrating tower import 51, dehydration overhead extraction mouth 52 and dehydrating tower kettle extraction are respectively equipped on the dehydrating tower 5
Mouth 56；Butanol tower feed inlet 61, butanol overhead extraction mouth 62 and butanol tower reactor extraction mouth 63 are respectively equipped on the butanol tower 6；
Falling film evaporator entrance 71 and falling film evaporator outlet 72 are respectively equipped on the falling film evaporator 7；The gas-liquid separator 8
On be respectively equipped with gas-liquid and divide device import 81, gas-liquid separator gaseous phase outlet 82 and gas-liquid separator liquid-phase outlet 83；The C5~
It is respectively equipped with the miscellaneous oily tower feed inlets 91 of C5~C8, the miscellaneous oily overhead extraction mouths 92 of C5~C8 and the miscellaneous oily towers of C5~C8 on the miscellaneous oily towers of C8 9
Kettle produces mouth 93；Octanol tower feed inlet 101, octanol overhead extraction mouth 102 and octanol tower reactor are respectively equipped on the octanol tower 10
Produce mouth 103.
The upper end of the reactor 3 is equipped with reactor gas phase import 32；The upper end of the knockout drum 4 is equipped with gas-liquid point
From tank gas phase import 41；The upper end of the dehydrating tower 5 is equipped with dehydration overhead extraction mouth 52, and the dehydration overhead extraction mouth 52 passes through
Pipeline is connected with oil-water decanter 53, and the left and right ends of the oil-water decanter 53 are respectively equipped with oil-water decanter material extraction mouth
54 and oil-water decanter waste water produce mouth 55；The upper end of the butanol tower 6 is equipped with butanol overhead extraction mouth 62；C5~the C8
The upper end of miscellaneous oil tower 9 is equipped with the miscellaneous oily overhead extraction mouths of C5~C8 92；The upper end of the octanol tower 10 is equipped with octanol overhead extraction mouth
102。
The lower end of the raw material pans 1 is equipped with raw material pans and exports 11, and raw material pans outlet 11 is passed through by pipeline
By the de- weight after the first raw material heat exchanger 34, the second raw material heat exchanger 12, feed preheater 13 and set on 2 side of the weight-removing column
Tower material inlet 21 is connected；The upper end of the weight-removing column 2 is equipped with weight-removing column top and produces mouth 23, and weight-removing column top produces mouth 23 and is set to
The reactor fluid inlet 31 of 3 top side of the reactor is connected by pipeline；The other side of the reactor 3 is equipped with reaction
Device gaseous phase outlet 36, reactor gaseous phase outlet 36 and the knockout drum gas phase import 41 for being set to 4 side of the knockout drum
Be connected by pipeline, the lower end of the reactor 3 is equipped with reactor liquid-phase outlet 33, the side of reactor liquid-phase outlet 33 with set
Knockout drum fluid inlet 42 in 4 side of the knockout drum is connected by pipeline, and the other side is by pipeline via the
One raw material heat exchanger 34, recycle stock heat exchanger 35 are connected with Reactor inlet 31；The lower end of the knockout drum 4 is equipped with gas
Liquid knockout drum liquid-phase outlet 43, knockout drum liquid-phase outlet 43 pass through pipeline and the dehydrating tower for being set to 5 side of the dehydrating tower
Material inlet 51 is connected；The lower part other side of the dehydrating tower 5 is equipped with dehydrating tower tower reactor and produces mouth 56, and dehydrating tower tower reactor produces mouth
56 are connected by pipeline with the butanol tower material inlet 61 set on 6 side of butanol tower, the lower part other side of the butanol tower 6
Mouth 63 is produced equipped with butanol tower reactor, butanol tower reactor produces mouth 63 and passes through pipeline and the falling liquid film for being set to 7 upper end of the falling film evaporator
Evaporator material inlet 71 is connected, and the lower end of the falling film evaporator 7 is equipped with falling film evaporator material outlet 72, falling film evaporator
Material outlet 72 is connected by pipeline with the gas-liquid separator material inlet 81 set on 8 side of the gas-liquid separator, the gas
The upper end of liquid/gas separator 8 is equipped with gas-liquid separator gaseous phase outlet 82, and gas-liquid separator gaseous phase outlet 82 is by pipeline and is set to institute
C5~C8 towers the material inlet 91 for stating miscellaneous oily 9 sides of tower C5~C8 is connected, and the lower part other side of the miscellaneous oily towers of the C5~C8 9 is equipped with
C5~C8 tower tower reactors produce mouth 93, C5~C8 tower tower reactors produce mouth 93 by pipeline be set to 10 side of octanol tower it is pungent
Alcohol tower material inlet 101 is connected, and the lower part side of the octanol tower 10 is equipped with octanol tower reactor and produces mouth 103, the extraction of octanol tower reactor
Mouth 103, the knockout drum liquid-phase outlet 83 set on 8 lower end of the gas-liquid separator, taking off set on 2 lower end of the weight-removing column
Weight tower reactor produces mouth 22 and removes heavy constituent tank after the second raw material heat exchanger 12 together by the way that pipeline is connected.
The weight-removing column, butanol tower, C5~C8 towers, octanol tower are negative pressure tower.
In addition, the utility model additionally provides a kind of technique that octyl alconyl raffinate recycles, include the following steps：
1) preparation：Introducing octyl alconyl raffinate to raw material pans 1, (octyl alconyl raffinate comes from butyl octanol unit, ingredient
For butanol, butyraldehyde, octenal, octanol, C5~C8, C12, C16 etc., each component content is varied from the condition of production), liquid level reaches
30-80%, raw material pans 1 are protected with N2 and (prevent material from reacting with air), and 1 operating pressure of raw material pans is
0.02-0.2Mpa；
2) weight is taken off：Material is pumped by raw material in raw material pans 1, and flowmeter is with flow with the speed of 1000~3000Kg/h
Through the first raw material heat exchanger 34 and reaction cycle material (material after octyl alconyl raffinate adds hydrogen, mainly butanol, octanol, C5~C8,
Deng) heat exchange, it exchanges heat with heavy component (C12, C16 etc.) through the second raw material heat exchanger 12, it is most pre- with steam through feed preheater 13 afterwards
Enter weight-removing column 2 after heat；Weight-removing column 2 is negative pressure tower, is -0.07~-0.09MPa, the condition that temperature is 40~195 DEG C in pressure
Under slough than octanol weight heavy component, overhead extraction have lighter component material (predominantly butyraldehyde, butanol, C5~C8, octenal,
Octanol etc.), it partly flows back, partial material enters reactor by pump.
3) hydrogenation reaction：Hydrogen from outer tube, which is forced by hydrogen compressor after 2.0~5.0Mpa, to be entered reactor 3 and leads to
Step 2) is crossed into the material in reactor 3, is carried out under conditions of pressure is 2.0~5.0Mpa, temperature is 60-160 DEG C anti-
It answers, the tower reactor extraction material (including butanol, octanol and C5~C8) of reactor 3 is partly recycled, through the first raw material heat exchanger
34 with raw material exchange heat, then through recycle stock cooler cooling after with reaction feed (reaction feed be weight-removing column top produce material,
Ingredient is butyraldehyde, butanol, C5~C8, octenal, octanol etc.) it is mixed into reactor 3, reaction feed is adjusted by recycle stock
The weight ratio of temperature and ingredient, recycle stock and reaction feed is 1：2~2：1 (preferably 1:1), the tower reactor part of reactor 3
Material is produced to knockout drum 4, and the liquid phase extraction of knockout drum 4 is to dehydrating tower, and the gas phase extraction of reactor 3 is through gas-liquid point
After being detached from tank 4, then emptying manifold is removed after cooling (including level-one water cooling and level-one ammonia cold)；
4) dehydrating tower rectifying：Material from knockout drum 4 enters dehydrating tower 5, pressure be 0.1MPa~
0.25MPa, temperature carry out rectifying under conditions of being 100~150 DEG C, a few materials such as butanol, trimethylheptane and water in material
Azeotropic goes waste water tank by overhead extraction, then by oil-water decanter water outlet, and butanol material returns to the recycling of raw material pans, trimethyl heptan
When the material contents such as alkane are accumulated to 50% or more, it can produce to miscellaneous oil tank (the miscellaneous oil product storage tanks of C5~C8), the tower reactor of dehydrating tower 5
Material produces pump extraction to butanol tower 6 by tower reactor；
5) rectifying of butanol tower and gas-liquid separator separates：Butanol tower 6 is -0.07~-0.09MPa, temperature 90 in pressure
Rectifying, overhead extraction butanol product are carried out under conditions of~140 DEG C, kettle material produces pump extraction to falling film evaporation by tower reactor
Device 7, lighter component material (main component is C5~C8, octanol) vaporization, liquid-vapor mixture material (fourth after the heating of falling film evaporator 7
Alcohol tower reactor produces material partial gasification) enter gas-liquid separator 8, liquid phase material (main component C12, C16) is used as heavy component
Extraction, gaseous phase materials enter the miscellaneous oily towers of C5~C8 9；
6) the miscellaneous oily tower rectifying of C5~C8：The miscellaneous oily towers of C5~C8 are -0.07~-0.09MPa in pressure, and temperature is 100~160
Rectifying is carried out under conditions of DEG C, the miscellaneous oil products of overhead extraction C5~C8 (predominantly butyl butyrate), kettle material is adopted by tower reactor
Go out pump extraction to octanol tower 10；
7) octanol tower rectifying：Octanol tower 10 is -0.07~-0.09MPa in pressure, under conditions of temperature is 120~190 DEG C
Rectifying is carried out, overhead extraction octanol products (purity is up to 99% or more), kettle material produces pump extraction by tower reactor, with de- weight
Tower reactor extraction, gas-liquid separator liquid phase extraction (main component C12, C16) are changed together as heavy component with by the second raw material
Heavy component tank (C12, C16 products pot) is removed after the raw material heat exchange of hot device 12.
Octyl alconyl raffinate hydrogenation reaction master equation is in the utility model：
The wherein described catalyst is carbon-based nickel-alumina catalyst (being purchased from Sinopec Beijing Chemical Research Institute).
After adding hydrogen, rectifying, device output butanol described in the utility model, octanol, the miscellaneous oil of C5~C8, heavy component etc.
Product, wherein butanol, octanol products purity can meet customer need up to 99% or more.
The above, the only preferable possible embodiments of the utility model, are not limited to the utility model
Range.
Claims (5)
1. the device that a kind of octyl alconyl raffinate recycles, which is characterized in that including sequentially connected raw material pans, de- weight
The miscellaneous oily tower of tower, reactor, knockout drum, dehydrating tower, butanol tower, falling film evaporator, gas-liquid separator, C5~C8 and octanol
Tower.
2. device as described in claim 1, which is characterized in that the raw material pans are exported equipped with raw material pans, institute
It states and is respectively equipped with weight-removing column material inlet, weight-removing column kettle extraction mouth and weight-removing column top extraction mouth on weight-removing column, on the reactor
It is respectively equipped with reactor fluid inlet, the import of reactor gas phase, reactor liquid-phase outlet and reactor gaseous phase outlet；The gas-liquid
The import of knockout drum gas phase, knockout drum fluid inlet, knockout drum liquid-phase outlet and gas are respectively equipped on knockout drum
Liquid knockout drum gaseous phase outlet；Dehydrating tower import, dehydration overhead extraction mouth and dehydrating tower kettle extraction are respectively equipped on the dehydrating tower
Mouthful；Butanol tower feed inlet, butanol overhead extraction mouth and butanol tower reactor extraction mouth are respectively equipped on the butanol tower；The falling liquid film steams
Falling film evaporator entrance and falling film evaporator outlet are respectively equipped on hair device；It is respectively equipped with gas-liquid on the gas-liquid separator and divides device
Import, gas-liquid separator gaseous phase outlet and gas-liquid separator liquid-phase outlet；It is respectively equipped with C5~C8 on the miscellaneous oily towers of the C5~C8
The miscellaneous oily overhead extraction mouth of miscellaneous oil tower feed inlet, C5~C8 and the miscellaneous oily tower reactors of C5~C8 produce mouth；It is respectively equipped on the octanol tower
Octanol tower feed inlet, octanol overhead extraction mouth and octanol tower reactor produce mouth.
3. device as described in claim 1, which is characterized in that the upper end of the reactor is equipped with reactor gas phase import；Institute
The upper end for stating knockout drum is equipped with knockout drum gas phase import；The upper end of the dehydrating tower is equipped with dehydration overhead extraction mouth,
The dehydration overhead extraction mouth is connected by pipeline with oil-water decanter, and the oil-water decanter is equipped with oil-water decanter material
It produces mouth and oil-water decanter waste water produces mouth；The upper end of the butanol tower is equipped with butanol overhead extraction mouth；C5~the C8 is miscellaneous
The upper end of oily tower is equipped with the miscellaneous oily overhead extraction mouths of C5~C8；The upper end of the octanol tower is equipped with octanol overhead extraction mouth.
4. device as described in claim 1, which is characterized in that the lower end of the raw material pans goes out equipped with raw material pans
Mouthful, raw material pans outlet by pipeline via after the first raw material heat exchanger, the second raw material heat exchanger, feed preheater be set to
The weight-removing column material inlet of the weight-removing column side is connected；The upper end of the weight-removing column is equipped with weight-removing column top and produces mouth, weight-removing column
Top extraction mouth is connected with the reactor fluid inlet set on reactor top side by pipeline；The reactor it is another
Side be equipped with reactor gaseous phase outlet, reactor gaseous phase outlet with set on the knockout drum side knockout drum gas phase into
Mouthful be connected by pipeline, the lower end of the reactor is equipped with reactor liquid-phase outlet, the side of reactor liquid-phase outlet be set to
The knockout drum fluid inlet of the knockout drum side is connected by pipeline, and the other side is by pipeline via the first raw material
Heat exchanger, recycle stock heat exchanger are connected with Reactor inlet；The lower end of the knockout drum is equipped with knockout drum liquid phase
Outlet, knockout drum liquid-phase outlet are connected by pipeline with the dehydrating tower material inlet set on the dehydrating tower side；It is described
The lower part other side of dehydrating tower is equipped with dehydrating tower tower reactor and produces mouth, and dehydrating tower tower reactor produces mouth by pipeline and is set to the butanol
The butanol tower material inlet of tower side is connected, and the lower part other side of the butanol tower is equipped with butanol tower reactor and produces mouth, butanol tower reactor
Extraction mouth is connected by pipeline with the falling film evaporator material inlet set on the falling film evaporator upper end, the falling film evaporator
Lower end be equipped with falling film evaporator material outlet, falling film evaporator material outlet by pipeline be set to the gas-liquid separator one
The gas-liquid separator material inlet of side is connected, and the upper end of the gas-liquid separator is equipped with gas-liquid separator gaseous phase outlet, gas-liquid point
It is connected with C5~C8 tower material inlets set on the miscellaneous sides You Ta the C5~C8 by pipeline from device gaseous phase outlet, the C5~
The lower part other side of the miscellaneous oily towers of C8 is equipped with C5~C8 tower tower reactors and produces mouth, and C5~C8 tower tower reactors produce mouth by pipeline and are set to institute
The octanol tower material inlet for stating octanol tower side is connected, and the lower part side of the octanol tower is equipped with octanol tower reactor and produces mouth, octanol
Tower reactor produces mouth, the knockout drum liquid-phase outlet set on the gas-liquid separator lower end, taking off set on the weight-removing column lower end
Weight tower reactor produces mouth and removes heavy constituent tank after the second raw material heat exchanger together by the way that pipeline is connected.
5. device as described in claim 1, which is characterized in that the reactor is liquid phase hydrogenation reactor；The weight-removing column,
The miscellaneous oily tower of butanol tower, C5~C8, octanol tower are negative pressure tower, and the charging of the miscellaneous oily towers of the C5~C8 is gas phase.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820122685.0U CN207877621U (en) | 2018-01-24 | 2018-01-24 | A kind of device that octyl alconyl raffinate recycles |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820122685.0U CN207877621U (en) | 2018-01-24 | 2018-01-24 | A kind of device that octyl alconyl raffinate recycles |
Publications (1)
| Publication Number | Publication Date |
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| CN207877621U true CN207877621U (en) | 2018-09-18 |
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