CN207537369U - A kind of ethylene glycol multi-effect distillation system - Google Patents
A kind of ethylene glycol multi-effect distillation system Download PDFInfo
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- CN207537369U CN207537369U CN201721400944.3U CN201721400944U CN207537369U CN 207537369 U CN207537369 U CN 207537369U CN 201721400944 U CN201721400944 U CN 201721400944U CN 207537369 U CN207537369 U CN 207537369U
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Abstract
The utility model is related to a kind of ethylene glycol multi-effect distillation systems, including sequentially connected dewatering unit, it is dehydrated treating column and product purification unit, the dewatering unit is the more than two dehydrating towers being sequentially communicated, the product purification unit is the more than two product purification towers being sequentially communicated, adjacent dehydration column overhead steam connects with the tower-coupled reboiler of next effect dehydration as the heat source of next effect dehydrating tower and forms economic benefits and social benefits and couples, the overhead vapours is after next effect is dehydrated tower-coupled reboiler heat exchange cooling, a part is back to former dehydration column overhead, another part produces, so as to complete the Mass and heat transfer in dehydrating tower tower；Adjacent product purification column overhead steam connects with next effect tower-coupled reboiler of product purification as the heat source of next effect product purification tower and forms economic benefits and social benefits and couples.
Description
Technical field
The utility model is related to a kind of ethylene glycol multi-effect distillation systems, belong to chemical materials purification field.
Background technology
Ethylene glycol, no color or smell, pleasantly sweet liquid, 197.3 DEG C of ethylene glycol boiling point, mankind lethal agent toxic to animal
Amount is about 1.6g/kg.Ethylene glycol can dissolve each other, but solubility is smaller in ethers with water, acetone.As solvent, antifreezing agent and
Synthesize the raw material of terylene.The high polymer polyethylene glycol (PEG) of ethylene glycol is a kind of phase transfer catalyst, is also used for cell fusion；
Its nitrate is a kind of explosive.
Rectifying is the mixed liquor that will be made of the different component of volatility, the carry out part multiple simultaneously in rectifying column
Vaporization and partial condensation separate it into the process of almost pure state component.
Material becomes steam after reboiler heats and rises in rectifying column in rectifying tower reactor, the phegma on every layer of column plate
Body is contacted with each other with upflowing vapor, carries out the transmittance process of heat and matter.Since there are temperature difference and concentration difference, gas phases on column plate
Partial condensation will be carried out, which part difficulty volatile component is made to be transferred in liquid phase；And the latent heat that vapor condensation releases is transmitted to liquid
Phase vaporizes liquid phase part, and which part volatile components are transferred in gas phase.The long and causes to leave the liquid phase of this layer of column plate
It is low when the concentration of middle volatile components is compared with into the plate, and the height that volatile components concentration relatively enters in the gas phase left.
If gas-liquid two-phase onboard time of contact long enough, then the gas-liquid two-phase for leaving the plate is mutually balance.Every laminate of rectifying column
On all carry out above-mentioned similar process.
In chemical industry, distillation process is one of unit operation of energy expenditure maximum, since global energy has occurred
Since source problem, the power saving of distillation process has caused the attention of people extensively.The energy saving of distillation process substantially can be with
Set about from following several respects：(1) distillation process thermal energy makes full use of；(2) distillation process is reduced in itself to the needs of energy；
(3) thermodynamic efficiency of distillation system is improved；(4) using qualified piece-rate system.
Energy saving technique of the multi-effect distillation as an emerging development, it is mainly with low energy consumption, and low-grade energy utilizes and height
Effect thermodynamic efficiency causes the great attention of people.Its theoretical research deepened continuously in recent years, applied in the industrial production
It is increasingly extensive.In advanced industrial country, multi-effect distillation has become a normative energy conserving system and is widely used in industrial production
In.Low energy consumption for multi-effect distillation, and good energy-conserving effect is used widely in production, and technical ability effect is demonstrate,proved by practice
It is real.
Utility model content
The utility model is in view of the deficienciess of the prior art, provide a kind of ethylene glycol multi-effect distillation system and technique side
Method.
The technical solution that the utility model solves above-mentioned technical problem is as follows：A kind of ethylene glycol multi-effect distillation system, including
Sequentially connected dewatering unit, dehydration treating column and product purification unit, the dewatering unit are the two or more being sequentially communicated
Dehydrating tower, the product purification unit is the more than two product purification towers being sequentially communicated, the first effect dehydrating tower, the
One effect product purification tower, dehydration treating column bottom of towe are equipped with the reboiler by external heat, the remaining dehydrating tower/product purification
Tower bottom of towe is equipped with through the coupling reboiler that the previous effect dehydrating tower/product purification column overhead steam is heat source, described adjacent
Dehydration column overhead steam connects with the tower-coupled reboiler of next effect dehydration as the heat source of next effect dehydrating tower and forms economic benefits and social benefits coupling
It closing, for the overhead vapours after next effect is dehydrated tower-coupled reboiler heat exchange cooling, a part is back to former dehydration column overhead,
Another part produces, so as to complete the Mass and heat transfer in dehydrating tower tower；The adjacent product purification column overhead is produced with next effect
Product refine tower-coupled reboiler and connect and form economic benefits and social benefits coupling, and product purification is tower-coupled boils again by next effect for the overhead vapours
After device heat exchange cooling, a part is back to original product and refines column overhead, another part extraction, so as to complete product purification Ta Tanei
Mass and heat transfer.
Further, the dewatering unit is fair current, and product purification unit is fair current, and the adjacent dehydrating tower bottom of towe is led to
It crosses pipeline with adjacent next effect dehydrating tower to be connected, last described effect dehydrating tower bottom of towe is refined by pipeline and the dehydration
Tower is connected, and the dehydration treating column bottom of towe is connected with the described first effect product purification tower, the adjacent product purification tower
Bottom of towe is connected by pipeline with adjacent next effect product purification tower, and it is de- that the raw material first charging aperture is located at the described first effect
Water tower.
Further, the dewatering unit is fair current, and product purification unit is adverse current, and the adjacent dehydrating tower bottom of towe is led to
It crosses pipeline with adjacent next effect dehydrating tower to be connected, last described effect dehydrating tower bottom of towe is refined by pipeline and the dehydration
Tower is connected, and the dehydration treating column bottom of towe is connected with last effect dehydration treating column, the adjacent product purification tower tower
Bottom is connected by pipeline with adjacent previous effect product purification tower, and the raw material first charging aperture is located at the described first effect and is dehydrated
Tower.
Further, the dewatering unit is adverse current, and product purification unit is adverse current, and the adjacent dehydrating tower bottom of towe is led to
It crosses pipeline with adjacent previous effect dehydrating tower to be connected, the first effect dehydrating tower bottom of towe passes through pipeline and the dehydration treating column
It is connected, the dehydration treating column bottom of towe is connected with last described effect product purification tower, the adjacent product purification tower
Bottom of towe is connected by pipeline with adjacent previous effect product purification tower, and the raw material first charging aperture is located at last described effect
Dehydrating tower.
Further, the feeding manner of the dehydrating tower, dehydration treating column and product purification tower is charging or tower in tower
Kettle feeds two ways.
Further, the dehydration treating column can be cancelled.
The utility model provides new process according to above system, which includes following three kinds：
1) a kind of, process of ethylene glycol multi-effect distillation, the process use ethylene glycol as claimed in claim 2
Multi-effect distillation system, which is dewatering unit fair current, refined unit fair current：
(1) raw material is fed by the first effect dehydrating tower, and raw material is in the first effect dehydration column reboiler heat temperature raising and vaporizes, and steams
Vapour rises to the tower top of the dehydrating tower；
(2) after next effect is dehydrated tower-coupled reboiler heat exchange cooling, part extraction, another part returns overhead vapours
The first effect dehydration column overhead is back to, so as to fulfill the Mass and heat transfer of the first effect tower top；
Raw material of the feedstock transportation of (3) first effect dehydrating tower bottom of towe to next effect dehydrating tower as next effect dehydrating tower, leads to
It crosses the coupling reboiler using the first dehydration column overhead steam as heat source and heats vaporization；
(4) after raw material sequentially enters last effect dehydrating tower, raw material is dehydrated tower-coupled reboiler through last effect and adds
Hot vapour, overhead vapours pass through the condenser condensation positioned at tower top, part extraction, and another part is back to tower top, completes tower
Interior Mass and heat transfer；The feedstock transportation of last effect dehydrating tower bottom of towe is to treating column is dehydrated, as the raw material for being dehydrated treating column；
(5) after raw material enters dehydration treating column, vaporization is heated by the reboiler for being dehydrated treating column bottom of towe, steam rises
Column overhead is refined to the dehydration, after overhead vapours is by being located at the condenser condensation of tower top, part extraction, another part returns
To the refined column overhead of dehydration, the Mass and heat transfer in tower is completed, the raw material positioned at bottom of towe is delivered to the first effect by bottom of towe delivery pump
Product purification tower, as first effect product purification tower raw material；
(6) raw material enters the first effect product purification tower, and the reboiler heating vaporization by bottom of towe, steam rises to tower
Then top cools down by the tower-coupled reboiler heat exchange of next effect product purification, part extraction, another part is back to the first effect
Product purification column overhead makes to complete Mass and heat transfer in tower；
The feedstock transportation of (7) first effect product purification tower bottom of towe to next effect product purification tower, charging is produced as next effect
The raw material of product treating column；
(8) after raw material sequentially enters last effect product purification tower, through last effect, product purification is tower-coupled boils again
Device heating vaporization, overhead vapours pass through the condenser condensation positioned at tower top, and part extraction, another part is back to tower top, complete
Into the Mass and heat transfer in tower；The kettle of last effect product purification tower bottom of towe is residual to drain into the residual tank of kettle.
2), the process is dewatering unit fair current, refined unit adverse current：
(1) raw material is fed by the first effect dehydrating tower, and raw material drops down onto tower reactor and imitates dehydration column reboiler heat temperature raising first
And vaporize, steam rises to the tower top of the dehydrating tower；
(2) after next effect is dehydrated tower-coupled reboiler heat exchange cooling, part extraction, another part returns overhead vapours
The first effect dehydration column overhead is back to, so as to fulfill the Mass and heat transfer of the first effect tower top；
The product of (3) first effect dehydrating tower bottom of towe is delivered to next effect dehydrating tower, as the raw material of next effect dehydrating tower, leads to
It crosses the coupling reboiler using the first dehydration column overhead steam as heat source and heats vaporization；
(4) after raw material sequentially enters last effect dehydrating tower, raw material is dehydrated tower-coupled reboiler through last effect and adds
Hot vapour, overhead vapours pass through the condenser condensation positioned at tower top, part extraction, and another part is back to tower top, completes tower
Interior Mass and heat transfer；The feedstock transportation of last effect dehydrating tower bottom of towe is to treating column is dehydrated, as the raw material for being dehydrated treating column；
(5) after raw material enters dehydration treating column, vaporization is heated by the reboiler for being dehydrated treating column bottom of towe, steam rises
Column overhead is refined to the dehydration, after overhead vapours is by being located at the condenser condensation of tower top, part extraction, another part returns
To the refined column overhead of dehydration, the Mass and heat transfer in tower is completed, the raw material positioned at bottom of towe is delivered to last by bottom of towe delivery pump
The product purification tower of effect, the raw material as last effect product purification tower；
(6) raw material enters last effect product purification tower, by bottom of towe with previous effect product purification column overhead steam
Coupling reboiler for heat source heats vaporization, and steam rises to tower top, and overhead vapours is after overhead condenser condensation cooling, and one
Part produces, and another part is back to last effect product purification column overhead, makes to complete Mass and heat transfer in tower；
(7) the supreme effect product purification tower of the feedstock transportation of last effect product purification tower bottom of towe, as upper one effect product
The raw material for the treatment of column；
(8) raw material of an effect product purification tower couples reboiler heating vaporization by upper one effect on, and steam rises to tower top,
For overhead vapours after last effect coupling reboiler heat exchange cooling, part extraction, another part is back to an effect product
Refined column overhead makes to complete Mass and heat transfer in tower；
(9) after raw material is sequentially entered to the first effect product purification tower, by the reboiler by external heat of bottom of towe
Heating vaporization, steam rise to tower top, and overhead vapours passes through the coupling reboiler heat exchange cooling for being located at next effect product purification tower
Afterwards, part extraction, another part are back to tower top, complete the Mass and heat transfer in tower；The kettle of first effect product purification tower bottom of towe
It is residual to produce to the residual tank of refined tower reactor.
3), the process is dewatering unit adverse current, refined unit adverse current：
(1) raw material by last effect dehydrating tower feed, raw material using it is previous effect dehydration column overhead steam as heat source most
Latter effect is dehydrated tower-coupled reboiler heat temperature raising and vaporizes, and steam rises to the tower top of the dehydrating tower；
(2) for overhead vapours after the condenser for being located at tower top cools down, part extraction, another part is back to last
Dehydration column overhead is imitated, so as to fulfill the Mass and heat transfer of last effect tower top；
(3) the supreme effect dehydrating tower of the feedstock transportation of last effect dehydrating tower bottom of towe, the raw material as upper one effect dehydrating tower；
(4) an effect dehydrating tower is dehydrated tower-coupled reboiler heating vaporization by upper one effect on, and steam rises to tower top, tower top
For steam after last effect coupling reboiler heat exchange cooling, part extraction a, part is back to an effect dehydration column overhead,
So as to fulfill the Mass and heat transfer of upper one effect dehydration column overhead；
(5) after raw material is sequentially entered to the first effect dehydrating tower, the reboiler heating vaporization by bottom of towe, steam rises to
Tower top, overhead vapours passes through carries out heat exchange cooling, part extraction positioned at the second tower-coupled reboiler of effect dehydration, and another part returns
Tower top is back to, completes the Mass and heat transfer in tower；The feedstock transportation of first effect dehydrating tower bottom of towe is to treating column is dehydrated, as dehydration essence
The raw material of tower processed；
(6) after raw material enters dehydration treating column, vaporization is heated by the reboiler for being dehydrated treating column tower reactor, steam rises
Column overhead is refined to the dehydration, after overhead vapours is by being located at the condenser condensation of tower top, part extraction, another part returns
Column overhead is refined to being dehydrated, the Mass and heat transfer in completion tower, the product purification tower imitated positioned at the feedstock transportation of bottom of towe to last,
Raw material as last effect product purification tower；
(7) raw material enters last effect product purification tower, by being heat by previous effect product purification column overhead steam
The bottom of towe coupling reboiler heating vaporization in source, steam rises to tower top, after overhead vapours is by being located at the condenser condensation of tower top,
Part extraction, another part are back to last effect product purification column overhead, make to complete Mass and heat transfer in tower；
(8) the supreme effect product purification tower of the feedstock transportation of last effect product purification tower bottom of towe, as upper one effect product
The raw material for the treatment of column；
(9) raw material of an effect product purification tower on passes through the tower-coupled reboiler heating vaporization of upper one effect product purification, steam
Tower top is risen to, overhead vapours is after the tower-coupled reboiler heat exchange cooling of last effect product purification, part extraction, another portion
Divide and be back to an effect product purification column overhead, complete the Mass and heat transfer in tower；
(10) after raw material is sequentially entered to the first effect product purification tower, by the first effect product purification tower reboiler heating
Vaporization, steam rise to tower top, and overhead vapours is after the coupling reboiler heat exchange cooling for being located at the second effect product purification tower, and one
Part produces, and another part is back to tower top, completes the Mass and heat transfer in tower；The residual extraction of kettle of first effect product purification tower bottom of towe
To the residual tank of refined tower reactor.
Advantageous effect：For the multi-effect distillation that the utility model uses compared with conventional distillation, water can be greatly reduced in multi-effect distillation
Steam consumption.If detaching a certain object system, when several rectification process may be used, the energy consumption of multi-effect distillation is generally than other essences
Evaporating that technique is low, multi-effect distillation can not only reduce the consumption of vapor, but also can also reduce the dosage and power consumption of cooling water,
Improve thermodynamic efficiency.Distillation process thermal energy is made full use of, reduces distillation process in itself to the needs of energy.Multiple-effect essence
The technical ability effect evaporated is affected by many factors, wherein the mainly property of separated object system, the content of volatile components, effect number
And technological process etc..Increase with effect number, energy consumption reduces, but effect number is more, and tower is more, and cost of equipment increases significantly.And it imitates
Number is more, and the energy-saving effect for often increasing by an effect is also lower and lower, therefore, in actual application, can not use excessive effect
Number, at most may be used seven effect rectifying.The product purification unit, dewatering unit of the utility model can carry out suitable according to actual conditions
Stream, adverse current, so as to substantially reduce energy consumption.
Description of the drawings
Fig. 1 is the technological process of a kind of dewatering unit fair current, refined unit fair current of the utility model；
Fig. 2 is a kind of dewatering unit fair current, the technological process of refined unit adverse current of the utility model；
Fig. 3 is the technological process of a kind of dewatering unit adverse current, refined unit adverse current of the utility model.
Specific embodiment
The principle and feature of the utility model are described below in conjunction with attached drawing, example is served only for explaining this practicality
It is novel, it is not intended to limit the scope of the utility model.
Embodiment one：
As shown in Figure 1, present embodiment relates to a kind of ethylene glycol multi-effect distillation system, it is single including sequentially connected dehydration
Member, dehydration treating column 8 and product purification unit, the dewatering unit are the more than two dehydrating towers being sequentially communicated, the production
Product refined unit is the more than two product purification towers being sequentially communicated, and the first effect dehydrating tower 1, first imitates product purification tower
11st, 8 bottom of towe of dehydration treating column is equipped with the reboiler 2,9,12 by external heat, the remaining dehydrating tower/product purification tower tower
Bottom is equipped with through the coupling reboiler that the previous effect dehydrating tower/product purification column overhead steam is heat source, the adjacent dehydration
Column overhead steam connects with the tower-coupled reboiler 4 of next effect dehydration as the heat source of next effect dehydrating tower 3 and forms economic benefits and social benefits and couples,
The overhead vapours is after next effect is dehydrated the tower-coupled heat exchange of reboiler 4 cooling, and a part is back to former dehydration column overhead, separately
Part extraction, so as to complete the Mass and heat transfer in dehydrating tower tower；Last described effect 5 overhead vapours of dehydrating tower is cold through tower top
After condenser cooling, part extraction, another part is back to the refined column overhead of dehydration, realizes the Mass and heat transfer of tower top；The phase
Adjacent product purification column overhead connects with next effect tower-coupled reboiler 14 of product purification and forms economic benefits and social benefits and couples, and the tower top steams
Vapour is after the tower-coupled heat exchange of reboiler 14 cooling of next effect product purification, and a part is back to original product and refines column overhead, separately
Part extraction, so as to complete the Mass and heat transfer of product purification Ta Tanei.
In present embodiment, the adjacent dehydrating tower bottom of towe is connected by pipeline with adjacent next effect dehydrating tower 3,
It is described last effect 5 bottom of towe of dehydrating tower by pipeline with it is described dehydration treating column 8 be connected, it is described dehydration 8 bottom of towe for the treatment of column and
The first effect product purification tower 11 is connected, and the adjacent product purification tower bottom of towe is produced by pipeline and adjacent next effect
Product treating column 13 is connected, and the raw material first charging aperture is located at the described first effect dehydrating tower 1.
The process for the ethylene glycol multi-effect distillation that the above system used in present embodiment one is implemented, the process
For dewatering unit fair current, refined unit fair current：
(1) raw material is fed by the first effect dehydrating tower 1, and raw material is in the first effect 1 reboiler heat temperature raising of dehydrating tower and vaporizes,
Steam rises to the tower top of the dehydrating tower；
(2) overhead vapours is after next effect is dehydrated the tower-coupled heat exchange of reboiler 4 cooling, part extraction, another part
1 tower top of the first effect dehydrating tower is back to, so as to fulfill the Mass and heat transfer of the first effect tower top；
Raw material of the feedstock transportation of (3) first effect 1 bottom of towe of dehydrating tower to next effect dehydrating tower 3 as next effect dehydrating tower 3,
The tower-coupled heating of reboiler 4 vaporization is dehydrated by next effect using the first dehydration column overhead steam as heat source；
(4) after raw material sequentially enters last effect dehydrating tower 5, raw material is dehydrated tower-coupled reboiler 6 through last effect
Heating vaporization, overhead vapours are condensed by the condenser 7 positioned at tower top, and part extraction, another part is back to tower top, completes
Mass and heat transfer in tower；The feedstock transportation of last effect 5 bottom of towe of dehydrating tower is to treating column 8 is dehydrated, as the original for being dehydrated treating column 8
Material；
(5) after raw material enters dehydration treating column 8, vaporization, steam are heated by the reboiler 9 for being dehydrated 8 bottom of towe for the treatment of column
8 tower top of dehydration treating column is risen to, after overhead vapours is by being located at the condensation of condenser 10 of tower top, part extraction is another
Part is back to dehydration 8 tower top for the treatment of column, completes the Mass and heat transfer in tower, and the raw material positioned at bottom of towe is conveyed by bottom of towe delivery pump
To the first effect product purification tower 11, the raw material as the first effect product purification tower 11；
(6) raw material enters the first effect product purification tower 11, and the heating vaporization of reboiler 12 by bottom of towe, steam rises to
Tower top, then by the tower-coupled reboiler 14 heat exchange cooling of next effect product purification, part extraction, another part is back to the
One effect product purification tower, 11 tower top, makes to complete Mass and heat transfer in tower；
The feedstock transportation of 11 bottom of towe of (7) first effect product purification tower is to next effect product purification tower 13, and charging is as next
Imitate the raw material of product purification tower 13；
(8) it is tower-coupled again through last effect product purification after raw material sequentially enters last effect product purification tower 15
The heating vaporization of device 16 is boiled, overhead vapours is condensed by the condenser 17 positioned at tower top, and part extraction, another part is back to tower
The Mass and heat transfer in tower is completed on top；The kettle of last 15 bottom of towe of effect product purification tower is residual to drain into the residual tank of kettle.
Embodiment two：
As shown in Fig. 2, present embodiment relates to a kind of ethylene glycol multi-effect distillation system, it is single including sequentially connected dehydration
Member, dehydration treating column 8 and product purification unit, the dewatering unit are the more than two dehydrating towers being sequentially communicated, the production
Product refined unit is the more than two product purification towers being sequentially communicated, and the first effect dehydrating tower 1, first imitates product purification tower
11st, 8 bottom of towe of dehydration treating column is equipped with the reboiler 2,9,12 by external heat, the remaining dehydrating tower/product purification tower tower
Bottom is equipped with through the coupling reboiler that the previous effect dehydrating tower/product purification column overhead steam is heat source, the adjacent dehydration
Column overhead steam connects with the tower-coupled reboiler 4 of next effect dehydration as the heat source of next effect dehydrating tower 3 and forms economic benefits and social benefits and couples,
The overhead vapours is after next effect is dehydrated the tower-coupled heat exchange of reboiler 4 cooling, and a part is back to former dehydration column overhead, separately
Part extraction, so as to complete the Mass and heat transfer in dehydrating tower tower；Last described effect 5 overhead vapours of dehydrating tower is cold through tower top
After condenser cooling, part extraction, another part is back to the refined column overhead of dehydration, realizes the Mass and heat transfer of tower top；The phase
Adjacent product purification column overhead connects with next effect tower-coupled reboiler 14 of product purification and forms economic benefits and social benefits and couples, and the tower top steams
Vapour is after the tower-coupled heat exchange of reboiler 14 cooling of next effect product purification, and a part is back to original product and refines column overhead, separately
Part extraction, so as to complete the Mass and heat transfer of product purification Ta Tanei.
In present embodiment two, the adjacent dehydrating tower bottom of towe is connected by pipeline with adjacent next effect dehydrating tower 3
Logical, last described effect 5 bottom of towe of dehydrating tower is connected by pipeline with the dehydration treating column 8, dehydration 8 bottom of towe for the treatment of column
It is connected with last effect dehydration treating column 8, the adjacent product purification tower bottom of towe is produced by pipeline and adjacent previous effect
Product treating column is connected, and the raw material first charging aperture is located at the described first effect dehydrating tower 1.
Using above system implement ethylene glycol multi-effect distillation process, the process for dewatering unit fair current,
Refined unit adverse current,
(1) raw material is fed by the first effect dehydrating tower 1, and raw material drops down onto tower reactor and risen in the first effect dehydrating tower 1 reboiler 2 heating
Temperature simultaneously vaporizes, and steam rises to the tower top of the dehydrating tower；
(2) overhead vapours is after next effect is dehydrated the tower-coupled heat exchange of reboiler 4 cooling, part extraction, another part
1 tower top of the first effect dehydrating tower is back to, so as to fulfill the Mass and heat transfer of the first effect 1 tower top of dehydrating tower；
The product of (3) first effect 1 bottom of towe of dehydrating tower is delivered to next effect dehydrating tower 3, the original as next effect dehydrating tower 3
Material is dehydrated the tower-coupled heating of reboiler 2 vaporization by the first effect using the first effect 1 overhead vapours of dehydrating tower as heat source；
(4) after raw material sequentially enters last effect dehydrating tower 5, raw material is dehydrated tower-coupled reboiler 6 through last effect
Heating vaporization, overhead vapours are condensed by the condenser 7 positioned at tower top, and part extraction, another part is back to tower top, completes
Mass and heat transfer in tower；The feedstock transportation of last effect 5 bottom of towe of dehydrating tower is to treating column 8 is dehydrated, as the original for being dehydrated treating column 8
Material；
(5) after raw material enters dehydration treating column 8, vaporization, steam are heated by the reboiler 9 for being dehydrated 8 bottom of towe for the treatment of column
8 tower top of dehydration treating column is risen to, after overhead vapours is by being located at the condensation of condenser 10 of tower top, part extraction is another
Part is back to dehydration 8 tower top for the treatment of column, completes the Mass and heat transfer in tower, and the raw material positioned at bottom of towe is conveyed by bottom of towe delivery pump
To last effect product purification tower 15, the raw material as last effect product purification tower 15；
(6) raw material enters last effect product purification tower 15, is steamed by bottom of towe with previous effect product purification column overhead
Coupling reboiler heating vaporization of the vapour for heat source, steam rise to tower top, and overhead vapours is by the condensation cooling of overhead condenser 17
Afterwards, part extraction, another part are back to last 15 tower top of effect product purification tower, make to complete Mass and heat transfer in tower；
(7) the supreme effect product purification tower of the feedstock transportation of last 15 bottom of towe of effect product purification tower, as upper one effect production
The raw material of product treating column；
(8) raw material of an effect product purification tower couples reboiler heating vaporization by upper one effect on, and steam rises to tower top,
After the tower-coupled heat exchange of reboiler 16 cooling of last effect product purification, part extraction, another part returns overhead vapours
Supreme effect product purification column overhead, makes to complete Mass and heat transfer in tower；
(9) after raw material is sequentially entered to the first effect product purification tower 11, by the boiling again by external heat of bottom of towe
The heating vaporization of device 12, steam rise to tower top, and overhead vapours passes through to exchange heat positioned at next effect tower-coupled reboiler 14 of product purification
After cooling, part extraction, another part is back to tower top, completes the Mass and heat transfer in tower；First effect product purification tower, 11 tower
The kettle at bottom is residual to be produced to the residual tank of refined tower reactor.
Embodiment three：
As shown in figure 3, present embodiment relates to a kind of ethylene glycol multi-effect distillation system, it is single including sequentially connected dehydration
Member, dehydration treating column 8 and product purification unit, the dewatering unit are the more than two dehydrating towers being sequentially communicated, the production
Product refined unit is the more than two product purification towers being sequentially communicated, and the first effect dehydrating tower 1, first imitates product purification tower
11st, 8 bottom of towe of dehydration treating column is equipped with the reboiler 2,9,12 by external heat, the remaining dehydrating tower/product purification tower tower
Bottom is equipped with through the coupling reboiler that the previous effect dehydrating tower/product purification column overhead steam is heat source, adjacent dehydrating tower tower
Top steam connects with the tower-coupled reboiler of next effect dehydration as the heat source of next effect dehydrating tower 3 and forms economic benefits and social benefits and couples, described
For overhead vapours after next effect dehydrating tower 3 couples reboiler heat exchange cooling, a part is back to former dehydration column overhead, another portion
Divide extraction, so as to complete the Mass and heat transfer in dehydrating tower tower；Last described effect 5 overhead vapours of dehydrating tower is through overhead condenser
After cooling, part extraction, another part is back to the refined column overhead of dehydration, realizes the Mass and heat transfer of tower top；It is described adjacent
Product purification column overhead connects with next effect tower-coupled reboiler 14 of product purification and forms economic benefits and social benefits and couples, the overhead vapours warp
After crossing the tower-coupled heat exchange of reboiler 14 cooling of next effect product purification, a part is back to original product and refines column overhead, another portion
Divide extraction, so as to complete the Mass and heat transfer of product purification Ta Tanei.
In embodiment three, the adjacent dehydrating tower bottom of towe is connected by pipeline with adjacent previous effect dehydrating tower
Logical, first effect 1 bottom of towe of dehydrating tower is connected by pipeline with the dehydration treating column 8, dehydration 8 bottom of towe for the treatment of column and
Last described effect product purification tower 15 is connected, and the adjacent product purification tower bottom of towe passes through pipeline and adjacent previous effect
Product purification tower is connected, and the raw material first charging aperture is located at last described effect dehydrating tower 5.
Using above system implement ethylene glycol multi-effect distillation process, the process for dewatering unit adverse current,
Refined unit adverse current：
(1) raw material by last effect dehydrating tower 5 feed, raw material using it is previous effect dehydration column overhead steam as heat source most
Latter effect is dehydrated tower-coupled 6 heat temperature raising of reboiler and vaporizes, and steam rises to the tower top of the dehydrating tower；
(2) after the condenser 7 for being located at tower top cools down, part extraction, another part is back to finally overhead vapours
One effect 5 tower top of dehydrating tower, so as to fulfill the Mass and heat transfer of last effect 5 tower top of dehydrating tower；
(3) the supreme effect dehydrating tower of the feedstock transportation of last effect 5 bottom of towe of dehydrating tower, the original as upper one effect dehydrating tower
Material；
(4) an effect dehydrating tower is dehydrated tower-coupled reboiler heating vaporization by upper one effect on, and steam rises to tower top, tower top
Steam is after last effect is dehydrated the tower-coupled heat exchange of reboiler 6 cooling, part extraction, and a part is back to an effect dehydration
Column overhead, so as to fulfill the Mass and heat transfer of upper one effect dehydration column overhead；
(5) after raw material is sequentially entered to the first effect dehydrating tower 1, the heating vaporization of reboiler 2 by bottom of towe, steam rises
To tower top, overhead vapours passes through carries out heat exchange cooling, part extraction, another portion positioned at the tower-coupled reboiler 4 of next effect dehydration
Divide and be back to tower top, complete the Mass and heat transfer in tower；The feedstock transportation of first effect 1 bottom of towe of dehydrating tower is extremely dehydrated treating column 8, as
It is dehydrated the raw material for the treatment of column 8；
(6) after raw material enters dehydration treating column 8, vaporization, steam are heated by the reboiler 9 for being dehydrated 8 tower reactor for the treatment of column
8 tower top of dehydration treating column is risen to, after overhead vapours is by being located at the condensation of condenser 10 of tower top, part extraction is another
Part be back to dehydration 8 tower top for the treatment of column, complete tower in Mass and heat transfer, positioned at bottom of towe feedstock transportation to last effect product
Treating column 15, the raw material as last effect product purification tower 15；
(7) raw material enters last effect product purification tower 15, by being by previous effect product purification column overhead steam
The bottom of towe coupling reboiler heating vaporization of heat source, steam rise to tower top, and overhead vapours is cold by the condenser 17 for being located at tower top
After solidifying, part extraction, another part is back to last 15 tower top of effect product purification tower, makes to complete Mass and heat transfer in tower；
(8) the supreme effect product purification tower of the feedstock transportation of last 15 bottom of towe of effect product purification tower, as upper one effect production
The raw material of product treating column；
(9) raw material of an effect product purification tower on passes through the tower-coupled reboiler heating vaporization of upper one effect product purification, steam
Tower top is risen to, for overhead vapours after the tower-coupled heat exchange of reboiler 16 cooling of last effect product purification, part extraction is another
Part is back to an effect product purification column overhead, completes the Mass and heat transfer in tower；
(10) after raw material is sequentially entered to the first effect product purification tower 11, by the first effect product purification tower reboiler 12
Heating vaporization, steam rise to tower top, and overhead vapours passes through the coupling reboiler heat exchange cooling for being located at the second effect product purification tower
Afterwards, part extraction, another part are back to tower top, complete the Mass and heat transfer in tower；First effect product purification tower, 11 bottom of towe
Kettle is residual to be produced to the residual tank of refined tower reactor.
In the three of the above embodiment of any one, the dehydrating tower, dehydration treating column 8 and product purification tower into
Material mode is that charging or tower reactor feed two ways in tower.
The above is only the preferred embodiment of the present invention, is not intended to limit the utility model, all in this practicality
Within novel spirit and principle, any modification, equivalent replacement, improvement and so on should be included in the guarantor of the utility model
Within the scope of shield.
Claims (6)
1. a kind of ethylene glycol multi-effect distillation system including sequentially connected dewatering unit, is dehydrated treating column and product purification unit,
It is characterized in that：The dewatering unit is the more than two dehydrating towers being sequentially communicated, and the product purification unit is connects successively
Logical more than two product purification towers, the first effect dehydrating tower, the first effect product purification tower, dehydration treating column bottom of towe are equipped with and pass through
The reboiler of external heat, the remaining dehydrating tower/product purification tower bottom of towe are equipped with through the previous effect dehydrating tower/product essence
Column overhead steam processed be heat source coupling reboiler, the adjacent dehydration column overhead steam as it is next effect dehydrating tower heat source with
Next tower-coupled reboiler of dehydration of imitating connects and forms economic benefits and social benefits coupling, and the overhead vapours boils again by next effect dehydration is tower-coupled
After device heat exchange cooling, a part is back to former dehydration column overhead, and another part extraction passes so as to complete the caloic in dehydrating tower tower
It passs；The adjacent product purification column overhead connects with next effect tower-coupled reboiler of product purification and forms economic benefits and social benefits and couples, institute
Overhead vapours is stated after the tower-coupled reboiler heat exchange cooling of next effect product purification, a part is back to original product treating column tower
Top, another part extraction, so as to complete the Mass and heat transfer of product purification tower tower.
2. a kind of ethylene glycol multi-effect distillation system according to claim 1, it is characterised in that：The dewatering unit is suitable
Stream, product purification unit are fair current, and the adjacent dehydrating tower bottom of towe is connected by pipeline with adjacent next effect dehydrating tower,
Last effect dehydrating tower bottom of towe is connected by pipeline with the dehydration treating column, the dehydration treating column bottom of towe and described first
Effect product purification tower is connected, and the adjacent product purification tower bottom of towe passes through pipeline and adjacent next effect product purification tower phase
Connection, raw material first charging aperture are located at the described first effect dehydrating tower.
3. a kind of ethylene glycol multi-effect distillation system according to claim 1, it is characterised in that：The dewatering unit is suitable
Stream, product purification unit are adverse current, and the adjacent dehydrating tower bottom of towe is connected by pipeline with adjacent next effect dehydrating tower,
Last effect dehydrating tower bottom of towe is connected by pipeline with the dehydration treating column, the dehydration treating column bottom of towe and last effect
Dehydration treating column is connected, and the adjacent product purification tower bottom of towe is connected by pipeline with adjacent previous effect product purification tower
Logical, raw material first charging aperture is located at the described first effect dehydrating tower.
4. a kind of ethylene glycol multi-effect distillation system according to claim 1, it is characterised in that：The dewatering unit is inverse
Stream, product purification unit are adverse current, and the adjacent dehydrating tower bottom of towe is connected by pipeline with adjacent previous effect dehydrating tower,
The first effect dehydrating tower bottom of towe is connected by pipeline with the dehydration treating column, described to be dehydrated treating column bottom of towe and last
Effect product purification tower is connected, and the adjacent product purification tower bottom of towe passes through pipeline and adjacent previous effect product purification tower phase
Connection, raw material first charging aperture are located at last described effect dehydrating tower.
5. according to a kind of ethylene glycol multi-effect distillation system described in any one of claim 1-4, it is characterised in that：The dehydration
The feeding manner of tower, dehydration treating column and product purification tower feeds two ways for charging in tower or tower reactor.
6. a kind of ethylene glycol multi-effect distillation system according to claim 5, it is characterised in that：The dehydration treating column can be with
Cancel.
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| CN201721400944.3U CN207537369U (en) | 2017-10-27 | 2017-10-27 | A kind of ethylene glycol multi-effect distillation system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110327647A (en) * | 2019-07-19 | 2019-10-15 | 张兵 | A kind of refining crude methanol process of three tower triple effect of modified |
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2017
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110327647A (en) * | 2019-07-19 | 2019-10-15 | 张兵 | A kind of refining crude methanol process of three tower triple effect of modified |
| CN110327647B (en) * | 2019-07-19 | 2021-12-10 | 张兵 | Improved three-tower three-effect crude methanol refining process method |
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