CN107473937A - A kind of method of withdrawal liquid chain fatty glycol - Google Patents
A kind of method of withdrawal liquid chain fatty glycol Download PDFInfo
- Publication number
- CN107473937A CN107473937A CN201710619779.9A CN201710619779A CN107473937A CN 107473937 A CN107473937 A CN 107473937A CN 201710619779 A CN201710619779 A CN 201710619779A CN 107473937 A CN107473937 A CN 107473937A
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- CN
- China
- Prior art keywords
- tower
- liquid
- temperature
- light ends
- feed liquid
- 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.)
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Classifications
-
- 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
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
- C07C41/40—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation
- C07C41/42—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation by distillation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of method of withdrawal liquid chain fatty glycol, is related to the field of material recycle and environmental protection, can continuously be reclaimed.The invention mainly includes steps：Feed liquid is delivered to preheater preheating, feed liquid after preheating enters tower among tower, when the feed liquid in tower reactor reaches 80%, heated by reboiler, liquid in tower from top to bottom, gas in tower from bottom to top, the bubbling on every block of column plate, transmission of heat by contact, control tower bottom, in tower, tower top temperature, the Light ends in feed liquid are made to reach boiling point, Light ends vapour phase exports from tower top, condensed into condenser, Light ends condensate liquid enters return tank from condenser bottom, a Light ends liquid part enters tower top as phegma in return tank, a part enters Light ends finished pot as finished product.According to bottom temperature, heavy component in tower reactor is delivered to heavy component finished pot by delivery pump.
Description
Technical field
The invention belongs to material recycle and field of Environment Protection, more particularly to a kind of method of withdrawal liquid chain fatty glycol.
Background technology
Dihydric alcohol effect is very extensive in modern chemical industry production, can be used as solvent, antifreezing agent and the raw material for synthesizing terylene
Deng.If the feed liquid discharge containing dihydric alcohol in Chemical Manufacture can cause environmental pollution, to improve the utilization of dihydric alcohol and preventing
Only environmental pollution need to carry out the recycling of dihydric alcohol.The recovery of traditional dihydric alcohol material is using distillation still, tower, cold
The equipment such as condenser carry out batch distillation, and material is disposably added in distillation still, and heating makes its vaporization, when kettle liquid group in distillation still
Into being stopped operation when reaching requirement, single flash operation is completed, and carries out distillation procedure next time, batch distillation operation treating capacity
It is small, be unfavorable for Automated condtrol, index does not have continuous-stable, energy consumption is higher, and have intermediate products in still-process, in
Between product need to be again introduced into distillation still and distilled, so batch distillation has some limitations.
The content of the invention
It the invention provides a kind of method of withdrawal liquid chain fatty glycol, can continuously be reclaimed, and be handled
Amount is big, it is possible to achieve Automated condtrol.
To reach above-mentioned purpose, the present invention adopts the following technical scheme that：
Feed liquid is delivered to preheater preheating by feed pump, and the feed liquid after preheating enters tower from tower, when in tower reactor
Feed liquid when reaching 80%, heated by reboiler, liquid by tower top from top to bottom, gas by tower bottom from bottom to top, every
Bubbling, transmission of heat by contact on block column plate, in control tower bottom, tower, tower top temperature, tower top temperature is higher than the boiling temperature of light component, made
Light ends in feed liquid reach boiling point, and Light ends vapour phase exports from tower top, is condensed into condenser, Light ends condensate liquid from
Condenser bottom enters return tank, and a Light ends liquid part enters tower top as phegma in return tank, a part of conduct into
Product enter Light ends finished pot.According to bottom temperature, heavy component in tower reactor is delivered to heavy component finished pot by delivery pump.
The low component of above step feed liquid mid-boiling point is that the high component of Light ends, boiling point is heavy component, the column bottom temperature
More than the temperature in the tower, the temperature in the tower is more than the temperature of the tower top.The temperature of the tower top is more than light component
Boiling point.When heavy component is the material containing two or more different boiling in tower reactor, heavy component passes through conveying in tower reactor
Pump is delivered to the continuous recovery process of next stage and recycled.
The beneficial effects of the invention are as follows：The invention provides a kind of method of withdrawal liquid chain fatty glycol, feed liquid can
Tower is pumped into continue through, interrupt operation process is not required to, is continuously reclaimed, it is possible to reduce intermediate product, and locate
Reason amount is big, it is possible to achieve Automated condtrol.
Brief description of the drawings
In order to illustrate more clearly of the technical scheme in the present invention, the required accompanying drawing used in the present invention will be made below
Simply introduce.
Fig. 1 is continuous distillation process schematic diagram in the present invention.
Fig. 2 is traditional batch distillation process schematic representation.
Embodiment
Embodiment 1
Water, ethylene glycol mixture material enter in tower after feed pump is delivered to preheater preheating, when the feed liquid in tower reactor reaches
When 80%, heated by reboiler, the water vapour after boiling in mixed material successively rises to tower top, and tower top uprising gas is through cold
Enter return tank after condenser condensation, when return tank liquid level reaches 30cm or so, squeezing into tower top by reflux pump is used as backflow.In vacuum
Under state, 81 DEG C or so of temperature, 75 DEG C or so of tower top temperature in 106 DEG C or so of column bottom temperature of control, tower, after temperature stabilization, one
Part water enters Light ends tank as the product that steam, and a part of water enters tower top as phegma, heavy constituent ethylene glycol by pump from by
Bottom of towe is discharged.Constantly entered by raw material in operation, water and ethylene glycol are constantly exported by pump, realize continuous operation.
Embodiment 2
Water, ethylene glycol, diethylene glycol mixed material enter in tower to tower reactor liquid level after feed pump is delivered to preheater preheating
80%, tower reactor is directly heated by reboiler steam, and the water vapour after boiling in mixed material successively rises to tower top, on tower top
Enter return tank after rising the condensation of gas condensed device, when return tank liquid level reaches 30cm or so, tower top conduct is squeezed into by reflux pump
Backflow.Under vacuum conditions, 81 DEG C or so of temperature, 75 DEG C or so of tower top temperature in 106 DEG C or so of column bottom temperature, tower, temperature are controlled
After degree is stablized, a part of water conduct steams product and enters Light ends tank, and a part of water enters tower top, heavy constituent as phegma（Second
Glycol, diethylene glycol mixture）By being pumped into the 80% of tower reactor liquid level in second set of tower, tower reactor is directly added by reboiler steam
Heat, the ethylene glycol after boiling in mixed material successively rise to tower top, enter backflow after the condensed device condensation of tower top uprising gas
Tank, when return tank liquid level reaches 30cm or so, squeezing into tower top by reflux pump is used as backflow.Under vacuum conditions, control tower bottom temperature
138 DEG C or so of temperature, 116 DEG C or so of tower top temperature in 198 DEG C or so of degree, tower, after temperature stabilization, a part of ethylene glycol is as steaming
Product enters Light ends tank, and a part of ethylene glycol enters tower top as phegma, and heavy constituent diethylene glycol is arranged by pump from by bottom of towe
Go out.Constantly entered by raw material in operation, water, ethylene glycol, diethylene glycol are constantly exported by pump, realize continuous operation.
Described above is only the preferred embodiment of the present invention, it should be pointed out that：For the ordinary skill people of the art
For member, under the premise without departing from the principles of the invention, some improvements and modifications can also be made, these improvements and modifications also should
It is considered as protection scope of the present invention.
Claims (4)
- A kind of 1. method of withdrawal liquid chain fatty glycol, it is characterised in that comprise the following steps：(1) feed liquid is delivered to preheater preheating；(2) feed liquid after preheating enters tower among tower；(3) when the feed liquid of tower reactor reaches 80%, feed liquid is heated；(4) liquid in tower from top to bottom, gas in tower from bottom to top, bubbling, transmission of heat by contact, control tower on every block of column plate In bottom, tower, tower top temperature, the Light ends in feed liquid is reached boiling point；(5) Light ends vapour phase exports from tower top, is condensed into condenser；(6) Light ends condensate liquid enters return tank from condenser bottom, and a Light ends liquid part is used as phegma in return tank Into tower top, a part enters Light ends finished pot as finished product；(7) according to bottom temperature, heavy component in tower reactor is delivered to heavy component finished pot by delivery pump；(8) if heavy component is the material containing two or more different boiling in tower reactor, heavy component passes through defeated in tower reactor Send pump to be delivered to the continuous recovery process of next stage to be recycled.
- 2. the method for withdrawal liquid chain fatty glycol according to claim 1, it is characterised in that step 2 passes through reboiler Heat feed liquid.
- 3. the method for withdrawal liquid chain fatty glycol according to claim 1, it is characterised in that the column bottom temperature is more than Temperature in the tower, the temperature in the tower are more than the temperature of the tower top.
- 4. according to the method for the withdrawal liquid chain fatty glycol of claim 1 or 3, it is characterised in that the tower top temperature Higher than the boiling temperature of light component.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710619779.9A CN107473937A (en) | 2017-07-26 | 2017-07-26 | A kind of method of withdrawal liquid chain fatty glycol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710619779.9A CN107473937A (en) | 2017-07-26 | 2017-07-26 | A kind of method of withdrawal liquid chain fatty glycol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107473937A true CN107473937A (en) | 2017-12-15 |
Family
ID=60598035
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710619779.9A Pending CN107473937A (en) | 2017-07-26 | 2017-07-26 | A kind of method of withdrawal liquid chain fatty glycol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107473937A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202214307U (en) * | 2011-09-21 | 2012-05-09 | 新疆美克化工股份有限公司 | 1,4-butanediol residual liquid recycling system |
| CN102807476A (en) * | 2012-07-27 | 2012-12-05 | 天津大学 | Method and device for continuous purification production of polyhydric alcohols |
| CN205933694U (en) * | 2016-07-08 | 2017-02-08 | 深圳市诚达科技股份有限公司 | 1, 3 purification device of propylene glycol |
| CN106946654A (en) * | 2017-03-29 | 2017-07-14 | 东华工程科技股份有限公司 | A kind of separation method of biomass ethylene glycol |
-
2017
- 2017-07-26 CN CN201710619779.9A patent/CN107473937A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202214307U (en) * | 2011-09-21 | 2012-05-09 | 新疆美克化工股份有限公司 | 1,4-butanediol residual liquid recycling system |
| CN102807476A (en) * | 2012-07-27 | 2012-12-05 | 天津大学 | Method and device for continuous purification production of polyhydric alcohols |
| CN205933694U (en) * | 2016-07-08 | 2017-02-08 | 深圳市诚达科技股份有限公司 | 1, 3 purification device of propylene glycol |
| CN106946654A (en) * | 2017-03-29 | 2017-07-14 | 东华工程科技股份有限公司 | A kind of separation method of biomass ethylene glycol |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20171215 |