CN108516924A - A kind of production system for high-purity fatty alcohol - Google Patents
A kind of production system for high-purity fatty alcohol Download PDFInfo
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- CN108516924A CN108516924A CN201810292772.5A CN201810292772A CN108516924A CN 108516924 A CN108516924 A CN 108516924A CN 201810292772 A CN201810292772 A CN 201810292772A CN 108516924 A CN108516924 A CN 108516924A
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- tower
- reaction
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- tank
- purity
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Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
- C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/88—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound
- C07C29/90—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound using hydrogen only
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of production systems for high-purity fatty alcohol, including aliphatic acid and catalyst blending tank and crude glycol tank, the crude glycol of the crude glycol tank is entered in the form of gas phase in reaction tower by being heated from reaction tower lower part through reboiler after tower reactor circulating pump and the mixing of tower reactor circulation fluid；The aliphatic acid and catalyst blending tank is pumped by fatty acid feedstock enters reaction tower from reaction tower top through packing layer in liquid form, and on filler surface, air-liquid two-phase comes into full contact with reaction, and it is cured to generate fat.Reasonable design of the present invention, controllability are strong, the higher natural acid of one side safety in utilization does not use the solid acid of safety difference, it is safe, on the other hand, product purity is high, and it is good that reaction distillation removes impurity effect, and high-efficiency washing is carried out to product, so that the cured impurity content of fat is extremely low, after adding hydrogen rectifying, product one pack system C6, C8, C10, C12 or 10 fatty alcohol purity of blending ingredients C8 reach 99.5% or more.
Description
Technical field
The present invention relates to a kind of production system of fatty alcohol more particularly to a kind of production systems for high-purity fatty alcohol
System.
Background technology
Low-carbon natural fatty alcohol (C6, C8, C10 or C8-10) is mainly used for the industries such as essence and flavoring agent, Premium detergents,
Impurity effect properties of product, general purity are more than 99.0%, and high purity product is more than 99.5%.It is higher to the purity requirement of product.
C6, C8, C10 alcohol are primarily present in cocounut oil or palm-kernel oil, ratio very little, expensive.In oil and fat refining, alcoholysis, methyl esters
The production processes such as rectifying, high-pressure hydrogenation, fatty alcohol rectifying, because the problems such as side reactions such as high temperature, oxidation and conversion ratio can not keep away
The generation exempted from contains hydro carbons（Such as alkane and alkene）, C=O classes（Such as aldehyde, ketone）The high C6-10 crude glycols of equal impurity contents, C6-10 are thick
Acid and the thick methyl esters of C6-10, these material impurity are higher, fatty alcohol（Or aliphatic acid, methyl esters）Content is less than 80%.In addition, fatty
Byproduct unsulfonated material purity is low obtained by alcohol sodium sulphate purifying technique, and C12 fatty alcohol contents about 80-90% can not directly make
With being purified.
Currently, purification is generally directly separated by rectifying according to boiling point difference, but some impurity and fatty alcohol boiling point are close
Then separating difficulty is very big, or even can not detach.Existing purification is high boiling solid by solid acid and fatty alcohol reaction generation
The fatty wax of body acid, impurity（Hydrocarbon, ester and C=O etc.）It is not involved in reaction, after the separation of high temperature decontamination, then the hydrolysis point of solid acid wax
From dehydration obtains high purity product.Solid acid toxic and volatile in this system, needs recycling device, and energy consumption is big, production limitation
In crude glycol raw material, yield is small, and through multiple high temp side reaction easily occurs for product.
Invention content
It is an object of the invention to：In view of the drawbacks of the prior art, it is proposed that a kind of production for high-purity fatty alcohol
System.
The technical solution adopted in the present invention is：A kind of production system for high-purity fatty alcohol, including aliphatic acid and
Catalyst blending tank, crude glycol tank, reaction tower, condenser, impurity collecting tank, tower reactor, reboiler and scrubbing tower, the crude glycol tank
Crude glycol by tower reactor circulating pump and tower reactor circulation fluid mixing after through reboiler heating from reaction tower lower part in the form of gas phase into
Enter in reaction tower；The aliphatic acid and catalyst blending tank by fatty acid feedstock pump from reaction tower top in liquid form into
Enter reaction tower through packing layer, air-liquid two-phase comes into full contact with reaction on filler surface, and it is cured to generate fat；The fat that reaction generates is cured
It is moved into tower reactor down, scrubbing tower is gone by the discharging of tower reactor circulating pump fraction, impurity and catalyst are removed by scrubbing tower,
Ensure that material is at stream mode is sieved when washing, not back-mixing；After the mixing of the crude glycol of most of material and crude glycol tank from feed system
It is heated by reboiler, the vaporization of crude glycol low boiling point up moves provides reaction kinetic energy for reaction, and nonvolatile fat is cured to enter tower
Kettle；Gas phase wherein in reaction process removes condenser from reaction tower top, and the slightly higher impurity of boiling point and a small amount of water cooling are congealed into liquid phase,
After being collected by impurity collecting tank, a portion controls the temperature of reaction tower top by reflux pump and return duct reflux, separately
Part discharging is used as byproduct.
In the present invention：Further include vacuum system, the vacuum system is connected with impurity collecting tank, through return duct and instead
It answers tower to be connected, the vacuum pressure of needs is provided for reaction, and remove reaction water, while reaction temperature is reduced by improving vacuum degree
It spends to prevent side reaction.
In the present invention：The charging of the end and aliphatic acid and catalyst blending tank of the return duct in reaction tower
The end of pipe is equipped with nozzle.
In the present invention：The upper and lower end of the reaction tower is equipped with filler, is equipped between two fillers and divides again
Cloth device prevents liquid phase wall stream, causes gas-liquid to exchange effect poor.
In the present invention：The scrubbing tower is internally provided with sieve plate, by sieve plate ensure wash when material at sieve stream mode,
Not back-mixing.
In the present invention：The top of the scrubbing tower is equipped with hot water piping, and the tower top of scrubbing tower is connected with plus hydrogen bead tube
Line；Fat that wherein reaction generates is cured to be entered from scrubbing tower lower part, is up moved because density is small, hot wash-water is from the upper of scrubbing tower
Portion enters to be moved down, and the fat by washing is cured to discharge from tower top, goes to add hydrogen rectifying after dehydrated cooled, required for finally obtaining
The each specification product of high-purity.
After adopting the above technical scheme, beneficial effects of the present invention are：Reasonable design of the present invention, controllability are strong, on the one hand
The higher liquid lower aliphatic acid of safety in utilization（Or methyl esters, ethyl ester class）It is safe without using solid acid, another party
Face, product purity is high, and reaction distillation removal impurity effect is good, and carries out high-efficiency washing to product so that the cured impurity content of fat
It is extremely low, after adding hydrogen rectifying, product one pack system C6, C8, C10, C12 or blending ingredients C8-10 fatty alcohol purity reach 99.5% with
On.
Description of the drawings
Fig. 1 is the system schematic of the present invention.
In figure：1, aliphatic acid and catalyst blending tank；2, fatty acid feedstock pumps；3, reaction tower；4, condenser；5, impurity is received
Collect tank；6, reflux pump；7, return duct；8, nozzle；9, filler；10, redistributor；11, tower reactor；12, tower reactor circulating pump；13、
Reboiler；14, crude glycol tank；15, crude glycol pumps；16, scrubbing tower；17, sieve plate；18, oil-water interfaces；19, scrubber overhead discharges.
Specific implementation mode
Below in conjunction with attached drawing, the present invention is further illustrated.
As seen from Figure 1, a kind of production system for high-purity fatty alcohol, including it is aliphatic acid and catalyst blending tank 1, thick
Alcohol tank 14, reaction tower 3, condenser 4, impurity collecting tank 5, tower reactor 11, reboiler 13 and scrubbing tower 16, the crude glycol tank 14
Crude glycol through reboiler 13 after tower reactor circulating pump 12 and the mixing of tower reactor circulation fluid by being heated to 140-300 DEG C from 3 lower part of reaction tower
Entered in the form of gas phase in reaction tower 3；Aliphatic acid in the aliphatic acid and catalyst blending tank 1（C6-12）And catalyst
Reaction tower 3 is entered by fatty acid feedstock pump 2 in liquid form from 3 top of reaction tower to 30-100 DEG C in blending tank mixing heat preservation
Through packing layer, reaction is come into full contact in 9 surface air-liquid two-phase of filler, it is cured to generate fat；The fat of reaction generation is cured to be moved down
Into tower reactor 11, scrubbing tower 16 is gone by the discharging of 12 fraction of tower reactor circulating pump, impurity and catalyst are removed by scrubbing tower 16,
Ensure that material is at stream mode is sieved when washing, not back-mixing；The mixing of the crude glycol of most of material and crude glycol tank 14 from feed system
Heated afterwards by reboiler 13, up movement provides reaction kinetic energy to the vaporization of crude glycol low boiling point to react, nonvolatile fat it is cured into
Enter tower reactor 11；The gas phase of impurity and vapor wherein in reaction process removes condenser 4 from the tower top of reaction tower 3, slightly boiling point
High impurity and a small amount of water cooling congeal into liquid phase, and after being collected by impurity collecting tank 5, a portion passes through reflux pump 6 and reflux
Pipe 7 flows back come the temperature for the tower top for controlling reaction tower 3, and another part discharging is used as auxiliary product.Wherein further include vacuum system, institute
The vacuum system stated is connected with impurity collecting tank 5, is connected with reaction tower 3 through return duct 7, and the vacuum pressure of needs is provided for reaction
Power, and reaction water is removed, while preventing side reaction by improving vacuum degree reduction reaction temperature.Wherein reaction tower tower
Push up temperature：50-150 DEG C, reaction tower bottom of tower liquidus temperature：100-240 DEG C, reaction tower tower top pressure：3-50KPa.
Gas phase（Impurity, water）Condenser 4 is removed from the tower top of reaction tower 3, the slightly higher impurity of boiling point and a small amount of water cooling are congealed into
Liquid phase, partial reflux control tower top temperature, and part discharging is used as auxiliary product.Reaction generate product boiling point height move down into
Enter tower reactor 11, scrubbing tower 16 is gone by the discharging of 12 fraction of tower reactor circulating pump.Most of material and crude glycol from feed system
It is heated by reboiler 13 after mixing, the vaporization of crude glycol low boiling point up moves provides reaction kinetic energy, nonvolatile fat for reaction
It is cured to enter tower reactor 11.
The material that reaction is completed enters the removal impurity and catalyst of 16 mesh of scrubbing tower, has sieve plate 17 inside scrubbing tower 16,
Ensure that material is at stream mode is sieved when washing, not back-mixing.Washing is completed under a certain pressure, and water vapor, washing effect is prevented to be deteriorated.
The tower top temperature of scrubbing tower 16：80-120 DEG C, pressure 200-300KPa（Gauge pressure）.The fat that reaction generates is cured under scrubbing tower 16
Portion enters system and is up moved because density is small, and hot wash-water enters from tower top to be moved down, is had sieve plate 17 among scrubbing tower 16, is protected
Exhibit material comes into full contact with.Fat by washing is cured to discharge from tower top, goes after dehydrated cooled plus hydrogen rectifying, required for finally obtaining
The each specification product of high-purity（C6, C8, C10, C12, C8-10 alcohol）.
The specific implementation mode of the present invention is described above, but the present invention is not limited to above description.For this
For the technical staff in field, any equal modification and replacement to the technical program is all within the scope of the invention.Cause
This, without departing from the spirit and scope of the invention made by impartial conversion and modification, all should be contained within the scope of the invention.
Claims (6)
1. a kind of production system for high-purity fatty alcohol, it is characterised in that：Including aliphatic acid and catalyst blending tank, crude glycol
The crude glycol of tank, reaction tower, condenser, impurity collecting tank, tower reactor, reboiler and scrubbing tower, the crude glycol tank is followed by tower reactor
Ring is pumped to be entered in the form of gas phase in reaction tower through reboiler heating from reaction tower lower part with after the mixing of tower reactor circulation fluid；Described
Aliphatic acid and catalyst blending tank are pumped by fatty acid feedstock enters reaction tower from reaction tower top through packing layer in liquid form,
On filler surface, air-liquid two-phase comes into full contact with reaction, and it is cured to generate fat；The fat of reaction generation is cured to be moved into tower reactor down,
Remove scrubbing tower by the discharging of tower reactor circulating pump fraction, impurity and catalyst removed by scrubbing tower, ensure when washing material at
Stream mode is sieved, not back-mixing；It is heated by reboiler after the mixing of the crude glycol of most of material and crude glycol tank from feed system, slightly
The vaporization of alcohol low boiling point up moves provides reaction kinetic energy for reaction, and nonvolatile fat is cured to enter tower reactor；Wherein in reaction process
Gas phase from reaction tower top remove condenser, the slightly higher impurity of boiling point and a small amount of water cooling are congealed into liquid phase, received by impurity collecting tank
After collection, a portion controls the temperature of reaction tower top by reflux pump and return duct reflux, and another part discharging is as secondary
Product.
2. a kind of production system for high-purity fatty alcohol according to claim 1, it is characterised in that：It further include vacuum
System, the vacuum system are connected with impurity collecting tank, are connected with reaction tower through return duct, and the vacuum of needs is provided for reaction
Pressure, and reaction water is removed, while preventing side reaction by improving vacuum degree reduction reaction temperature.
3. a kind of production system for high-purity fatty alcohol according to claim 1, it is characterised in that：It is described to be located at instead
The end of the end and the feed pipe of aliphatic acid and catalyst blending tank of answering the return duct in tower is equipped with nozzle.
4. a kind of production system for high-purity fatty alcohol according to claim 1, it is characterised in that：The reaction
The upper and lower end of tower is equipped with filler, is equipped with redistributor between two fillers, prevents liquid phase wall stream, gas-liquid is caused to exchange
Effect is poor.
5. a kind of production system for high-purity fatty alcohol according to claim 1, it is characterised in that：The washing
Tower is internally provided with sieve plate, ensures that material is at stream mode is sieved when washing by sieve plate, not back-mixing.
6. a kind of production system for high-purity fatty alcohol according to claim 1, it is characterised in that：The scrubbing tower
Top be equipped with hot water piping, the tower top of scrubbing tower is connected with plus hydrogen rectifying pipeline；The fat that wherein reaction generates is cured from washing
Tower lower part enters, and is up moved because density is small, and hot wash-water enters from the top of scrubbing tower to be moved down, by the fat of washing
It is cured to discharge from tower top, it goes to add hydrogen rectifying after dehydrated cooled, finally obtains each specification product of required high-purity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810292772.5A CN108516924A (en) | 2018-03-30 | 2018-03-30 | A kind of production system for high-purity fatty alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810292772.5A CN108516924A (en) | 2018-03-30 | 2018-03-30 | A kind of production system for high-purity fatty alcohol |
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| Publication Number | Publication Date |
|---|---|
| CN108516924A true CN108516924A (en) | 2018-09-11 |
Family
ID=63431174
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810292772.5A Pending CN108516924A (en) | 2018-03-30 | 2018-03-30 | A kind of production system for high-purity fatty alcohol |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1990008123A1 (en) * | 1989-01-17 | 1990-07-26 | Davy Mckee (London) Limited | Process |
| US5157168A (en) * | 1989-01-17 | 1992-10-20 | Davy Mckee (London) Limited | Process for the production of fatty alcohols |
| WO1994010112A1 (en) * | 1992-10-29 | 1994-05-11 | Davy Mckee (London) Limited | Process for the production of fatty alcohols |
| EP0612710A1 (en) * | 1993-02-13 | 1994-08-31 | METALLGESELLSCHAFT Aktiengesellschaft | Method of controlling the amount of used catalyst to be recycled to a hydrogenation reactor, used to produce fatty alcohols from fatty acids, or their derivatives |
| CN103282335A (en) * | 2011-11-17 | 2013-09-04 | 戴维加工技术有限公司 | Process for producing fatty alcohols from fatty acids |
| CN104703955A (en) * | 2012-10-09 | 2015-06-10 | 约翰逊·马泰·戴维技术有限公司 | Process for the production of a fatty alcohol from a fatty acid |
| CN105418364A (en) * | 2014-09-12 | 2016-03-23 | 乔治·克劳德方法的研究开发空气股份有限公司 | Process and plant for producing fatty alcohols |
-
2018
- 2018-03-30 CN CN201810292772.5A patent/CN108516924A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1990008123A1 (en) * | 1989-01-17 | 1990-07-26 | Davy Mckee (London) Limited | Process |
| US5157168A (en) * | 1989-01-17 | 1992-10-20 | Davy Mckee (London) Limited | Process for the production of fatty alcohols |
| WO1994010112A1 (en) * | 1992-10-29 | 1994-05-11 | Davy Mckee (London) Limited | Process for the production of fatty alcohols |
| EP0612710A1 (en) * | 1993-02-13 | 1994-08-31 | METALLGESELLSCHAFT Aktiengesellschaft | Method of controlling the amount of used catalyst to be recycled to a hydrogenation reactor, used to produce fatty alcohols from fatty acids, or their derivatives |
| CN103282335A (en) * | 2011-11-17 | 2013-09-04 | 戴维加工技术有限公司 | Process for producing fatty alcohols from fatty acids |
| CN104703955A (en) * | 2012-10-09 | 2015-06-10 | 约翰逊·马泰·戴维技术有限公司 | Process for the production of a fatty alcohol from a fatty acid |
| CN105418364A (en) * | 2014-09-12 | 2016-03-23 | 乔治·克劳德方法的研究开发空气股份有限公司 | Process and plant for producing fatty alcohols |
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Application publication date: 20180911 |
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