CN108245915A - A kind of azeotropic distillation separator - Google Patents
A kind of azeotropic distillation separator Download PDFInfo
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- CN108245915A CN108245915A CN201810304488.5A CN201810304488A CN108245915A CN 108245915 A CN108245915 A CN 108245915A CN 201810304488 A CN201810304488 A CN 201810304488A CN 108245915 A CN108245915 A CN 108245915A
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- azeotropic
- light phase
- pipeline
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- 238000010533 azeotropic distillation Methods 0.000 title claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 114
- 230000008676 import Effects 0.000 claims abstract description 25
- 238000004821 distillation Methods 0.000 claims abstract description 23
- 238000007599 discharging Methods 0.000 claims description 6
- 238000013459 approach Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 239000012071 phase Substances 0.000 description 183
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 28
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 12
- 238000000926 separation method Methods 0.000 description 12
- 239000000203 mixture Substances 0.000 description 8
- 239000002904 solvent Substances 0.000 description 6
- 239000000470 constituent Substances 0.000 description 5
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 239000012074 organic phase Substances 0.000 description 4
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- 101150038956 cup-4 gene Proteins 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000007667 floating Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- -1 and after separation Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 238000013517 stratification Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/02—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in boilers or stills
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a kind of azeotropic distillation separators,Including distillation still,Condenser,Azeotropic liquid receiving vessel,Azeotropic liquid import is equipped in the middle part of azeotropic liquid receiving vessel,The bottom of azeotropic liquid receiving vessel is equipped with heavy out,Top is equipped with light phase export,Heavy out is connected with heavy phase container by heavy phase pipeline,Light phase export is connected with light phase container by light phase pipeline,The position of heavy phase container and light phase container is below heavy out,The position of heavy phase pipeline peak is less than light phase export,Light phase density is D1,Heavy phase density is D2,Difference in height between light phase export and heavy out is H1,Difference in height between heavy phase pipeline peak and heavy out is H2,Light phase and the heavy phase pressure at heavy out reach balance,Meet H1 D1=H2 D2,Content of the light phase in azeotropic liquid is a,Content of the heavy phase in azeotropic liquid is b,Difference in height between azeotropic liquid import and heavy out is H3,H3=a H1 or H3=（1‑b）•H1.
Description
Technical field
The present invention relates to a kind of azeotropic distillation separators, for detaching two kinds of immiscible solvents, belong to chemical industry and set
Standby technical field.
Background technology
Azeotropic distillation method is commonly used a kind of operating method in chemical process, is according to water and certain organic molten
Agent it is incompatible, but the property of azeotropic mixture can be formed, water and organic solvent be distilled from system together, azeotropic component
It can be layered after being condensed into liquid after leaving Distallation systm, respectively obtain water and organic solvent.It can be to being using azeotropic distillation
System is concentrated, is dehydrated（The water and the water of reaction generation brought into including raw material）Deng operation, and the azeotropic of most of azeotropic mixture
Point is all relatively low, more particularly suitable to the product of certain not resistant against high temperatures, therefore azeotropic distillation piece-rate system is obtained in chemical field
It is widely applied.
Traditional intermittent separator is as shown in Figure 1, it includes distillation still 1 and is arranged on the condensation of 1 top of distillation still
Device 2, condenser lower section are equipped with azeotropic liquid receiving vessel 3, and the pipeline of 3 bottom of azeotropic liquid receiving vessel is equipped with baiting valve and regarding cup
4, the lower section being located on pipeline depending on cup 4 is parallel with heavy phase container 5 and light phase container 6.The operating process of the separator is：It comes from
The condensed device 2 of azeotropic mixture of distillation still 1 enters azeotropic liquid receiving vessel 3 after condensing, distillation terminates latter two liquid in azeotropic liquid
Stratification in receiving vessel 3 controls liquid to flow out, first with heavy phase container 5 by the baiting valve of 3 bottom of azeotropic liquid receiving vessel
Collect the big liquid of density（Hereinafter referred to as heavy phase or heavy constituent）, by being observed depending on cup 4, it is seen that and after two-phase interface, then density is small
Liquid（Hereinafter referred to as light phase or light component）It is collected into light phase container 6.This separator is intermittent operation, and there are following
Shortcoming：（1）Azeotropic liquid receiving vessel needs to accommodate the heavy phase and light phase all steamed, needs larger volume, occupies more space；
（2）Stratification is needed after distillation, it can only intermittently operated；（3）The time is needed to wait for after distillation, when expending a large amount of
Between, utilization rate of equipment and installations is low；（4）When two-phase is all colourless transparent liquid, boundary is missed unless you give your whole attention to it, material can only be returned
It returns and detaches again.
There are a kind of improved separator, this improved separator on the basis of the intermittent separator of Fig. 1
As shown in Fig. 2, it includes distillation still 1 and is arranged on the condenser 2 of 1 top of distillation still, being equipped with azeotropic liquid below condenser receives
Container 3, the condensate liquid pipeline on condenser are passed through from 3 middle part of azeotropic liquid receiving vessel in azeotropic liquid receiving vessel 3, and azeotropic liquid connects
3 bottom of receptor is connect by heavy phase pipeline with heavy phase container 5, and heavy phase pipeline is equipped with heavy phase baiting valve 71 and heavy phase regards cup
41, azeotropic liquid receiving vessel top is connect by light phase pipeline with light phase container 6, and light phase pipeline is equipped with 72 He of light phase baiting valve
Light phase regards cup 42.The operational process of the separator is：Condensed azeotropic liquid is entered from the middle part of azeotropic liquid receiving vessel 3
（Also have from top to stretch into pipe in container and be inserted to middle part, principle is identical）, azeotropic liquid receiving vessel 3 receives condensed fluid
When, heavy phase sinks, and light phase is observed depending on cup 41 by the heavy phase of 3 bottom of azeotropic liquid receiving vessel, estimated according to evaporation capacity toward floating
It calculates, the produced quantity that heavy phase valve 71 controls heavy constituent can be adjusted, and according to total liquid level, open light phase valve 72 and collect light group
Point, the produced quantity of the observation light component of cup 42 is regarded by light phase, it is basic to realize continuous operation.As notification number for CN205182727,
The Chinese patent of CN205832683 belongs to this one kind.
This improvement type separator of Fig. 2 solves the problems, such as space hold compared with the intermittent separator of Fig. 1,
Azeotropic liquid receiving vessel is commonly made to asthenic, and weight, light phase is allowed to have enough disengaging times, and the volume of receiving vessel even can be with
As low as original 1/10th, but still have the following disadvantages：（1）During separation must very important person keep an eye on, pay attention to light phase and heavy phase
Produced quantity, in time open and adjustment related valve；（2）Two-phase interface in azeotropic liquid receiving vessel can not perceive（Unless with
Glass be made but glass container often safety cannot be guaranteed, do not considered in being commonly designed）, operating personnel are difficult to judge to hold
Easy maloperation；（3）In addition, notification number is to be pointed out in the Chinese patent of CN205832683：" the extraction pipeline section 24 of water is less than toluene
The height of return duct 50 " is only limitted to the small solvent of segregation ratio water density（Such as toluene, ethyl acetate）, purposes is by certain
Limitation, and the concrete numerical value not yet explicitly " being less than ".
Invention content
The automatic azeotropic kept an eye on steaming is not needed to when detaching light phase and heavy phase liquid the purpose of the present invention is to provide a kind of
Separator is evaporated, to solve the problems, such as that the azeotropic distillation separator of prior art needs manually keep an eye on two-phase interface.
The present invention adopts the following technical scheme that：A kind of azeotropic distillation separator including distillation still and is arranged on distillation still
The condenser of top, condenser lower section are equipped with azeotropic liquid receiving vessel, and azeotropic liquid import is equipped in the middle part of azeotropic liquid receiving vessel, cold
Condensate liquid pipeline is equipped between condenser and azeotropic liquid import, the bottom of azeotropic liquid receiving vessel is equipped with heavy out, top is equipped with
Light phase export, heavy out are connected with heavy phase container by heavy phase pipeline, and light phase export is connected with light phase by light phase pipeline to be held
The position of device, heavy phase container and light phase container is below heavy out, and the heavy phase pipeline first rises one section and is passed through weight still further below
In phase container, the position of heavy phase pipeline peak is less than light phase export, and light phase density is D1, heavy phase density D2, light phase export
Difference in height between heavy out is H1, and the difference in height between heavy phase pipeline peak and heavy out is H2, light phase and again
Mutually pressure reaches balance at heavy out, that is, meets H1D1=H2D2, and content of the light phase in azeotropic liquid is a, heavy phase
Content in azeotropic liquid is b, the difference in height between azeotropic liquid import and heavy out for H3, H3=aH1 or H3=（1-b）·
H1。
The heavy phase pipeline includes the first horizontal segment being connected on heavy out, and it is perpendicular that first is connected in first horizontal segment
Straight section, the height of the first vertical section is H2, is connected with the second horizontal segment in the first vertical section, is connected with and is passed through on the second horizontal segment
To the second vertical section in heavy phase container；The light phase pipeline includes being connected to light phase horizontal segment on light phase export, and light phase is horizontal
It is connected in section and is passed into light phase vertical section in light phase container.
It is located in first vertical section and the second vertical section at identical height and position and is respectively equipped with rotary joint, rotates
First vertical section and the second vertical section are respectively classified into two parts up and down by connector, and upper part is assemblied in down by rotary joint rotation
On part.
Difference in height between the rotary joint and heavy out is equal to 1/2 H1, and first vertical section and second is vertically
The rotation angle of the upper part of section is respectively less than 90 °.
Second horizontal segment is equipped with blow-down pipe.
Dirt discharging valve is connected in the first horizontal segment.
The azeotropic liquid import is conical opening of the protrusion outside azeotropic liquid receiving vessel, and conical opening is along the azeotropic liquid side of entrance
To gradual increase, the condensate liquid pipeline is connected on conical opening.
The quantity of the conical opening is two, and two conical openings are arranged at intervals up and down.
The height of the azeotropic liquid receiving vessel is more than 5 with diameter ratio.
The beneficial effects of the invention are as follows：In the middle part of azeotropic liquid receiving vessel in the present invention height of azeotropic liquid import be according to
What the content of azeotropic composition species light phase and heavy phase was designed, adapt to the separation of the solvent and water of various density sizes.Altogether
During boiling, heavy phase and light phase are simultaneously into azeotropic liquid receiving vessel, due to azeotropic distillation initial stage and later stage, azeotropic composition be have compared with
Big difference.There are two extreme situations for azeotropic distillation：Distillate only has heavy constituent or only light component.At distillation initial stage, each appearance
Device and pipeline are all empty, and method is first to inject heavy phase into azeotropic liquid receiving vessel, until azeotropic liquid entrance location.If from steaming
It is entirely heavy phase to evaporate distilled out in kettle, because the position of heavy phase pipeline peak is less than light phase export, in azeotropic liquid receiving vessel
Heavy phase liquid level rising when reaching the height of heavy phase pipeline peak, heavy phase could be flowed into heavy phase container；If from distillation still
What is distilled out is entirely light phase, and with the progress of distillation process, light phase continuously enters azeotropic liquid receiving vessel, by heavy phase
It squeezes away, two-phase interface moves down, and two-phase fluid column static pressure reaches balance when reaching heavy out, and heavy phase will not continue to flow out, light phase
Liquid level just reaches the height of light phase export and flows into light phase container through light phase pipeline.The present invention no matter azeotropic distillation initial stage
Or the later stage, can effectively, accurately divide water, by adjusting heavy phase pipeline peak height can realize adapt to different densities size
Solvent（Certainly, it is necessary that the density contrast between weight, light phase, which is more than 0.1, is the important parameter of azeotropic distillation）.The present invention can be with
Realization automatically continuously divides water, controls without valve and manually keeps an eye on.
Preferably, by setting rotary joint respectively in two vertical sections of heavy phase pipeline, upper part can be connect with rotation
Head is rotated for axis, according to heavy phase and the density of light phase, adjusts the pressure that the size of H2 makes two-phase at first horizontal segment
Reach balance, the height of rotary joint is set as the half of H1, rotation angle≤90 °, for the two-phase of D2/D1=1.1 ~ 2
It is automatically separated with realizing.
Preferably, the second horizontal segment is equipped with blow-down pipe and can avoid generating siphon.
Preferably, the dirt discharging valve in first horizontal segment can be used for emptying extraction raffinate in pipe when maintenance or system solution change,
And it is non-automatic, continuously divide needed for water.
Preferably, azeotropic liquid import is conical opening, since conical opening gradually increases along azeotropic liquid approach axis, azeotropic composition
Object, which enters in conical opening, has begun to " heavy phase sinking " and the separation process of " light phase floating ", so that point of heavy phase and light phase
From more thorough, separation faster.
Preferably, two azeotropic liquid imports up and down are set, and when organic phase density ratio water is small, such as toluene-aqueous systems, water is attached most importance to
Liquid in condenser is passed through the azeotropic liquid import of lower part by phase, and after separation, water enters heavy phase container, toluene enters light phase appearance
Device；When organic phase density ratio water is big, such as chlorobenzene-aqueous systems, then water is light phase, and the liquid in condenser is passed through to the azeotropic on top
Liquid import, after separation, chlorobenzene enters heavy phase container, water enters light phase container.
Preferably, the height of azeotropic liquid receiving vessel is more than 5 with diameter ratio, it is ensured that two-phase has in azeotropic liquid receiving vessel
Enough residence times, reach desired separating effect, specific volume can be set according to azeotropic vaporization amount and residence time
Meter.
Description of the drawings
Fig. 1 is the structure diagram of the intermittent azeotropic distillation separator of the prior art；
Fig. 2 is a kind of structure diagram of improvement type azeotropic distillation separator of the prior art；
Fig. 3 is the structure diagram of an embodiment of the present invention；
Fig. 4 is the sectional view of light phase pipeline and heavy phase pipeline in Fig. 3；
Fig. 5 is the structure diagram of azeotropic liquid receiving vessel in another embodiment of the invention.
In figure, 1- distillation stills, 2- condensers, 3- azeotropic liquid receiving vessels, 31- azeotropic liquid imports, 32- light phase exports, 33-
Heavy out, 4- regard cup, 41- heavy phases regard cup, 42- light phases regard cup, 5- heavy phase containers, 6- light phase containers, 71- heavy phase valves,
72- light phase valves, 8- light phase pipelines, 9- heavy phase pipelines, 10- rotary joints, 11- blow-down pipes, 12- dirt discharging valves.
Specific embodiment
The present invention is described in detail with specific embodiment below in conjunction with the accompanying drawings.
The structure of an embodiment of the present invention as shown in Figure 3 and Figure 4, the azeotropic distillation separator of the present embodiment, including
Distillation still 1 and the condenser 2 for being arranged on 1 top of distillation still, 2 lower section of condenser are equipped with azeotropic liquid receiving vessel 3, and azeotropic liquid receives
3 middle part of container is equipped with azeotropic liquid import 31, and condensate liquid pipeline, the azeotropic liquid are equipped between condenser 2 and azeotropic liquid import 31
Conical opening of the import 31 for protrusion outside azeotropic liquid receiving vessel 3, conical opening gradually increases along azeotropic liquid approach axis, described
Condensate liquid pipeline is connected on conical opening.
The height of the azeotropic liquid receiving vessel 3 is more than 5 with diameter ratio, it is ensured that two-phase has foot in azeotropic liquid receiving vessel
Enough residence times, reach desired separating effect, specific volume can be designed according to azeotropic vaporization amount and residence time.
The bottom of azeotropic liquid receiving vessel 3 is equipped with heavy out 33, top is equipped with light phase export 32, and heavy out 33 passes through
Heavy phase pipeline 9 is connected with heavy phase container 5, and light phase export 32 is connected with light phase container 6 by light phase pipeline 8, heavy phase container 5 and light
The position of phase container 6 is below heavy out 33, and the heavy phase pipeline 9 first rises one section and is passed through still further below in heavy phase container 5, weight
The position of 9 peak of phase pipeline is less than light phase export 32, and light phase density is D1, heavy phase density D2, light phase export 32 and heavy phase
Difference in height between outlet 33 is H1, and the difference in height between 9 peak of heavy phase pipeline and heavy out 33 is H2, light phase and heavy phase
Pressure reaches balance at heavy out 33, that is, meets H1D1=H2D2 or H1/H2=D2/D1, light phase is in azeotropic liquid
Content is a, and content of the heavy phase in azeotropic liquid is b, a+b=1, and the difference in height between azeotropic liquid import 31 and heavy out 33 is
H3, H3=aH1 or H3=1-bH1.
In the present embodiment, the heavy phase pipeline 9 includes the first horizontal segment L3 being connected on heavy out 33, first level
The first vertical section is connected on section L3, the height of the first vertical section is equal to H2, the second horizontal segment L2 is connected in the first vertical section,
The second vertical section being passed into heavy phase container 5 is connected on second horizontal segment L2；The light phase pipeline 8 includes being connected to light phase
It is connected on light phase horizontal segment L1 in outlet 32, light phase horizontal segment L1 and is passed into light phase vertical section in light phase container 6.Described first
It is located in vertical section and the second vertical section at identical height and position and is respectively equipped with rotary joint 10, rotary joint 10 is erected first
Straight section and the second vertical section are respectively classified into two parts up and down, and upper part is assemblied in by the rotation of rotary joint 10 in lower part.Institute
State rotary joint 10 and heavy phase 33 export between difference in height be equal to 1/2 H1, first vertical section and the second vertical section it is upper
Partial rotation angle is respectively less than 90 °.
Second horizontal segment L2 of heavy phase pipeline is equipped with blow-down pipe 11, can avoid generating siphon.First water of heavy phase pipeline
Dirt discharging valve 12 is connected on flat section L3, dirt discharging valve can be used for emptying extraction raffinate in pipe when maintenance or system solution change, and non-automatic,
Continuously divide needed for water.
In the middle part of azeotropic liquid receiving vessel in the present invention height of azeotropic liquid import be according to azeotropic composition species light phase and
What the content of heavy phase was designed, adapt to the separation of the solvent and water of various density sizes.
During azeotropic, heavy phase and light phase enter azeotropic liquid receiving vessel by azeotropic liquid import simultaneously, and azeotropic liquid import is taper
Mouthful, since conical opening gradually increases along azeotropic liquid approach axis, azeotropic constituent, which enters in conical opening, have been begun to " under heavy phase
It is heavy " and " light phase floatings " separation process, so that the separation of heavy phase and light phase is more thorough, detaches faster.Since azeotropic steams
Initial stage and later stage are evaporated, azeotropic composition has bigger difference.There are two extreme situations for azeotropic distillation：Distillate only has heavy constituent
Or only light component.At distillation initial stage, each container and pipeline are all empty, and method is that weight is first injected into azeotropic liquid receiving vessel
Phase, until azeotropic liquid entrance location.If what is distilled out from distillation still is entirely heavy phase, because the position of heavy phase pipeline peak is low
When heavy phase liquid level rising in light phase export, azeotropic liquid receiving vessel reaches the height of heavy phase pipeline peak, heavy phase ability
It flows into heavy phase container；If what is distilled out from distillation still is entirely light phase, with the progress of distillation process, light phase is continually
Ground enters azeotropic liquid receiving vessel, and heavy phase is squeezed away, and two-phase interface moves down, and two-phase fluid column static pressure reaches when reaching heavy out
Balance, heavy phase will not continue to flow out, and light phase liquid level just reaches the height of light phase export and flows into light phase container through light phase pipeline.
By setting rotary joint respectively in two vertical sections of heavy phase pipeline, upper part can be using rotary joint as axis
It is rotated, according to heavy phase and the density of light phase, the pressure that adjusting the size of H2 makes two-phase at first horizontal segment reaches balance,
The height of rotary joint is set as the half of H1, and rotation angle≤90 ° can realize certainly the two-phase of D2/D1=1.1 ~ 2
Dynamic separation.As shown in figure 4, L2（H）When being that the second horizontal segment L2 is in highest order, the second horizontal segment L2 and first horizontal segment L3's
Difference in height is H2（H）, the H1 equal to 0.9 times；L2（O）When being that the second horizontal segment L2 is in interposition, the second horizontal segment L2 and
The difference in height of one horizontal segment L3 is H2（O）；L2（L）When being that the second horizontal segment L2 is in lowest order, the second horizontal segment L2 and first
The difference in height of horizontal segment L3 is H2（L）.
The present invention no matter at the initial stage or later stage of azeotropic distillation, can effectively, accurately divide water, by adjusting heavy phase pipeline most
The height of high point can realize the solvent for adapting to different densities size（Certainly, it is necessary that the density contrast between weight, light phase, which is more than 0.1,
, be azeotropic distillation important parameter）.The present invention, which can realize, automatically continuously divides water, controls without valve and manually keeps an eye on.
In other embodiments of the invention, the quantity of conical opening is can be two, as shown in figure 5, two conical openings
It is arranged at intervals up and down.Setting two azeotropic liquid imports up and down, when organic phase density ratio water is small, such as toluene-aqueous systems, water is attached most importance to
Liquid in condenser is passed through the azeotropic liquid import of lower part by phase, and after separation, water enters heavy phase container, toluene enters light phase appearance
Device；When organic phase density ratio water is big, such as chlorobenzene-aqueous systems, then water is light phase, and the liquid in condenser is passed through to the azeotropic on top
Liquid import, after separation, chlorobenzene enters heavy phase container, water enters light phase container.
Claims (9)
1. a kind of azeotropic distillation separator, including distillation still（1）Be arranged on distillation still（1）The condenser of top（2）, condensation
Device（2）Lower section is equipped with azeotropic liquid receiving vessel（3）, azeotropic liquid receiving vessel（3）Middle part is equipped with azeotropic liquid import（31）, condenser
（2）With azeotropic liquid import（31）Between be equipped with condensate liquid pipeline, azeotropic liquid receiving vessel（3）Bottom be equipped with heavy out
（33）, top be equipped with light phase export（32）, heavy out（33）Pass through heavy phase pipeline（9）It is connected with heavy phase container（5）, light phase goes out
Mouthful（32）Pass through light phase pipeline（8）It is connected with light phase container（6）, heavy phase container（5）With light phase container（6）Position be below weight
Mutually export（33）, it is characterised in that：The heavy phase pipeline（9）First rise one section and be passed through heavy phase container still further below（5）It is interior, heavy phase pipe
Road（9）The position of peak is less than light phase export（32）, light phase density be D1, heavy phase density D2, light phase export（32）With again
Mutually export（33）Between difference in height for H1, heavy phase pipeline（9）Peak and heavy out（33）Between difference in height for H2, gently
Mutually and heavy phase is in heavy out（33）Place's pressure reaches balance, that is, meets H1D1=H2D2, light phase containing in azeotropic liquid
It measures as a, content of the heavy phase in azeotropic liquid is b, azeotropic liquid import（31）And heavy out（33）Between difference in height be H3, H3
=aH1 or H3=（1-b）·H1.
2. azeotropic distillation separator according to claim 1, it is characterised in that：The heavy phase pipeline（9）Including connection
In heavy out（33）On first horizontal segment（L3）, first horizontal segment（L3）On be connected with the first vertical section, the first vertical section
Height be equal to H2, be connected with the second horizontal segment in the first vertical section（L2）, the second horizontal segment（L2）On be connected be passed into weight
Phase container（5）In the second vertical section；The light phase pipeline（8）Including being connected to light phase export（32）Upper light phase horizontal segment
（L1）, light phase horizontal segment（L1）On be connected with and be passed into light phase container（6）Middle light phase vertical section.
3. azeotropic distillation separator according to claim 2, it is characterised in that：First vertical section and second is vertically
It is located in section at identical height and position and is respectively equipped with rotary joint（10）, rotary joint（10）First vertical section and second are erected
Straight section is respectively classified into two parts up and down, and upper part passes through rotary joint（10）Rotation is assemblied in lower part.
4. azeotropic distillation separator according to claim 3, it is characterised in that：The rotary joint（10）With heavy phase
（33）Difference in height between outlet is equal to 1/2 H1, and the rotation angle of the upper part of first vertical section and the second vertical section is equal
Less than 90 °.
5. azeotropic distillation separator according to claim 2, it is characterised in that：Second horizontal segment（L2）It is equipped with
Blow-down pipe（11）.
6. azeotropic distillation separator according to claim 2, it is characterised in that：The first horizontal segment（L3）Upper connection
Dirt discharging valve（12）.
7. the azeotropic distillation separator according to claim 1 to 6 any one, it is characterised in that：The azeotropic liquid into
Mouthful（31）It is protrusion in azeotropic liquid receiving vessel（3）External conical opening, conical opening gradually increase along azeotropic liquid approach axis, institute
Condensate liquid pipeline is stated to be connected on conical opening.
8. azeotropic distillation separator according to claim 7, it is characterised in that：The quantity of the conical opening is two,
Two conical openings are arranged at intervals up and down.
9. the azeotropic distillation separator according to claim 1 to 6 any one, it is characterised in that：The azeotropic liquid connects
Receptor（3）Height and diameter ratio be more than 5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810304488.5A CN108245915A (en) | 2018-04-08 | 2018-04-08 | A kind of azeotropic distillation separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810304488.5A CN108245915A (en) | 2018-04-08 | 2018-04-08 | A kind of azeotropic distillation separator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108245915A true CN108245915A (en) | 2018-07-06 |
Family
ID=62747870
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810304488.5A Pending CN108245915A (en) | 2018-04-08 | 2018-04-08 | A kind of azeotropic distillation separator |
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| Country | Link |
|---|---|
| CN (1) | CN108245915A (en) |
Citations (11)
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| CN203139691U (en) * | 2013-03-29 | 2013-08-21 | 王朋 | Light/heavy phase material separation device |
| CN203816274U (en) * | 2014-05-17 | 2014-09-10 | 齐鲁安替（临邑）制药有限公司 | Extraction demixer for producing imipenem drugs |
| WO2017208082A1 (en) * | 2016-05-30 | 2017-12-07 | Energia Tech S.R.O | Gravity separation system, gravity separation vessel and method for separating a mixed liquid |
| CN208426669U (en) * | 2018-04-08 | 2019-01-25 | 江苏凌云药业股份有限公司 | A kind of azeotropic distillation separator |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| DD205074A2 (en) * | 1983-12-21 | APPARATUS FOR THE CONTINUOUS SEPARATION OF NON-MIXABLE FLUIDS | ||
| CN1048808A (en) * | 1989-07-20 | 1991-01-30 | 里克特吉迪恩韦耶斯泽提贾尔公司 | The equipment that liquids having different specific weight is in contact with one another |
| CN201454162U (en) * | 2009-07-10 | 2010-05-12 | 湖北益泰药业有限公司 | Oil-water automatic separating device for distillation |
| CN201775985U (en) * | 2010-08-24 | 2011-03-30 | 江苏依柯化工有限公司 | Automatic solvent-water separator |
| CN102059000A (en) * | 2010-11-08 | 2011-05-18 | 南通天泽化工有限公司 | Automatic draining device with oscillation extraction column for producing 3-cyanopyridine |
| CN102380229A (en) * | 2011-08-23 | 2012-03-21 | 常州市华人化工有限公司 | Continuous extraction device and continuous extraction method adopting same |
| CN202682847U (en) * | 2012-05-29 | 2013-01-23 | 广州南沙龙沙有限公司 | Device capable of realizing biphase continuous separation of nicotinamide |
| CN203139691U (en) * | 2013-03-29 | 2013-08-21 | 王朋 | Light/heavy phase material separation device |
| CN203816274U (en) * | 2014-05-17 | 2014-09-10 | 齐鲁安替（临邑）制药有限公司 | Extraction demixer for producing imipenem drugs |
| WO2017208082A1 (en) * | 2016-05-30 | 2017-12-07 | Energia Tech S.R.O | Gravity separation system, gravity separation vessel and method for separating a mixed liquid |
| CN208426669U (en) * | 2018-04-08 | 2019-01-25 | 江苏凌云药业股份有限公司 | A kind of azeotropic distillation separator |
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