CN206631232U - Energy-saving type vacuum flash distillation device - Google Patents
Energy-saving type vacuum flash distillation device Download PDFInfo
- Publication number
- CN206631232U CN206631232U CN201720149182.8U CN201720149182U CN206631232U CN 206631232 U CN206631232 U CN 206631232U CN 201720149182 U CN201720149182 U CN 201720149182U CN 206631232 U CN206631232 U CN 206631232U
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- Prior art keywords
- tank
- dichlorohenzene
- heat exchanger
- mother liquor
- energy
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- 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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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a kind of energy-saving type vacuum flash distillation device, including o-dichlorohenzene mother liquor tank, scrapper thin film evaporator, rectifying column, apply mechanically o-dichlorohenzene tank, settling tank and slag charge kettle, o-dichlorohenzene mother liquor tank is sequentially connected mother liquor tank transfering material pump by pipeline, First Heat Exchanger, scrapper thin film evaporator and rectifying column, the gas outlet of rectifying column is sequentially connected First Heat Exchanger by pipeline, second heat exchanger, first gas-liquid separator, apply mechanically o-dichlorohenzene tank and settling tank, the bottom discharge mouth of scrapper thin film evaporator is sequentially connected slag charge kettle and slag case by pipeline, the gas outlet of first gas-liquid separator is sequentially connected the first surge tank by pipeline, first vavuum pump, first pans and the 3rd heat exchanger.The utility model is applied to the distillation recovery of permanent violet o-dichlorohenzene mother liquor, and technological operation is simple, take up an area less, organic efficiency is high, energy consumption is low, and maintenance of equipment rate is low.
Description
Technical field
It the utility model is related to solvent recovery technical field, and in particular to a kind of energy-saving type vacuum flash distillation device.
Background technology
In the production process of synthesis permanent violet, 3- nitro-N- ethyl carbazoles are in o-dichlorohenzene as in the system of solvent
The mixture of 3- amino-N- ethyl carbazoles and o-dichlorohenzene is obtained after being reduced, mixture enters condensation kettle o-dichlorohenzene
After dilution, under sodium acetate alkalescence condition, condensation reaction is carried out with tetrachloroquinone.Condensation product is transferred to closed loop kettle, is taken advantage of after closed loop
Heat filtering, filtrate are the mixture of o-dichlorohenzene and side reaction impurity, and filter cake is washed with o-dichlorohenzene, then is washed with pull open powder,
For diafiltration liquid after precipitation, lower floor is the mother liquor of aqueous o-dichlorohenzene.
Because organic pigment has the characteristics of being insoluble in solvent and larger specific surface area, in order to ensure the adequacy of stirring,
So the usage amount of solvent is larger during the course of the reaction, filter cake needs to be washed with o-dichlorohenzene in addition, so 1 ton of permanent violet of production
Aqueous o-dichlorohenzene mother liquor is at 25 tons or so caused by crude product.
In order to reduce the discharge of the consumption of o-dichlorohenzene and waste residue, the mode of enterprise's generally use reactor simple distillation,
But a small amount of pull open powder is dissolved because yield is larger, and in water-bearing mother liquor, still-process easily spumes, and causes kettle batch
Distillation amount is less, is only capable of 2/5 volume held using kettle.In addition, in the still-process after waste residue is criticized or accumulated to kettle, in order to steam
Only, usual time dragsaw is longer.
For the quality of pigment, and avoid washing o-dichlorohenzene dosage caused by the o-dichlorohenzene content that feeds intake is too low
Increased vicious circle, the o-dichlorohenzene content that usual o-dichlorohenzene mother liquor obtains after single flash be 96.5%, now need through
Second distillation is crossed, content could be improved to more than 97.8%.
So efficiency, quality that the distillation recovery of o-dichlorohenzene mother liquor is applied mechanically are the bottleneck of production, wherein retracting device
Occupation of land and energy consumption can all influence the cost of product.
The content of the invention
To solve the deficiencies in the prior art, the purpose of this utility model be to provide a kind of technological operation is simple, take up an area less,
Organic efficiency is high, energy consumption is low, and the energy-saving type vacuum flash distillation device that maintenance of equipment rate is low.
In order to realize above-mentioned target, the utility model adopts the following technical scheme that：
Energy-saving type vacuum flash distillation device, including o-dichlorohenzene mother liquor tank, scrapper thin film evaporator, rectifying column, apply mechanically
O-dichlorohenzene tank, settling tank and slag charge kettle, o-dichlorohenzene mother liquor tank are sequentially connected mother liquor tank transfering material pump, the first heat exchange by pipeline
Device, scrapper thin film evaporator and rectifying column, the gas outlet of rectifying column are sequentially connected First Heat Exchanger, the second heat exchange by pipeline
Device, the first gas-liquid separator, apply mechanically o-dichlorohenzene tank and settling tank, the bottom discharge mouth of scrapper thin film evaporator by pipeline according to
Secondary connection slag charge kettle and slag case, the gas outlet of the first gas-liquid separator are sequentially connected the first surge tank, first true by pipeline
Empty pump, the first pans and the 3rd heat exchanger.
Preferably, flowmeter is additionally provided between foregoing mother liquor tank transfering material pump and First Heat Exchanger, it is adjustable to be changed into first
The amount of o-dichlorohenzene mother liquor in hot device.
More preferably, the bottom side of foregoing settling tank is provided with discharging opening, and discharging opening is connected by settling tank transfering material pump to be covered
With o-dichlorohenzene tank.
It is highly preferred that the top side of foregoing slag case is provided with exhaust outlet, exhaust outlet connection device for absorbing tail gas, can avoid
Pollute environment.
Specifically, foregoing slag charge kettle is sequentially connected the 4th heat exchanger, the second gas-liquid separator, the second buffering by pipeline
Tank, the second vavuum pump, the second pans and the 5th heat exchanger.
Preferably, foregoing second gas-liquid separator is sequentially connected the 3rd pans and middle transfering material pump by pipeline.
More preferably, foregoing slag charge kettle includes cylinder, chuck and agitating device located at cylinder body outer wall, and agitating device includes
Motor in the middle part of cylinder top and the puddler located at inner barrel.
It is highly preferred that foregoing o-dichlorohenzene mother liquor tank, to apply mechanically o-dichlorohenzene tank and the quantity of slag charge kettle be two, two
It is used alternatingly.
It is of the present utility model to be beneficial in that：The utility model distilling apparatus is applied to permanent violet o-dichlorohenzene mother liquor
It is distilled to recover, its technological operation is simple, take up an area less, organic efficiency is high, energy consumption is low, and the o-dichlorohenzene content for distilling to obtain is reachable
More than 97.8%, and using continuous feed distillation mode, the temperature deformation of equipment is less, and maintenance of equipment rate is low.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
The implication of reference in figure：1st, o-dichlorohenzene mother liquor tank, 2, scrapper thin film evaporator, 3, rectifying column, 4, apply mechanically
O-dichlorohenzene tank, 5, settling tank, 6, slag charge kettle, 7, mother liquor tank transfering material pump, 8, First Heat Exchanger, 9, flowmeter, the 10, second heat exchange
Device, the 11, first gas-liquid separator, 12, settling tank transfering material pump, 13, slag case, 14, exhaust outlet, the 15, first surge tank, 16,
One vavuum pump, the 17, first pans, the 18, the 3rd heat exchanger, the 19, the 4th heat exchanger, the 20, second gas-liquid separator, 21, second
Surge tank, the 22, second vavuum pump, the 23, second pans, the 24, the 5th heat exchanger, the 25, the 3rd pans, 26, middle transfering material pump,
27th, standby o-dichlorohenzene mother liquor tank, 28, it is standby apply mechanically o-dichlorohenzene tank, 29, apply mechanically o-dichlorohenzene tank transfering material pump, 30, standby slag
Expect kettle.
Embodiment
Make specific introduce to the utility model below in conjunction with the drawings and specific embodiments.
Energy-saving type vacuum flash distillation device of the present utility model, including o-dichlorohenzene mother liquor tank 1, scrapper thin film evaporator
2nd, rectifying column 3, apply mechanically o-dichlorohenzene tank 4, settling tank 5 and slag charge kettle 6.O-dichlorohenzene mother liquor tank 1 is sequentially connected mother by pipeline
Flow container transfering material pump 7, First Heat Exchanger 8, scrapper thin film evaporator 2 and rectifying column 3, mother liquor tank transfering material pump 7 and First Heat Exchanger 8 it
Between be additionally provided with flowmeter 9, can adjust enter First Heat Exchanger 8 in o-dichlorohenzene mother liquor amount.The gas outlet of rectifying column 3 passes through
Pipeline is sequentially connected First Heat Exchanger 8, the second heat exchanger 10, the first gas-liquid separator 11, applies mechanically o-dichlorohenzene tank 4 and settling tank
5, discharging opening is provided with the bottom side of settling tank 5, discharging opening applies mechanically o-dichlorohenzene tank 4 by the connection of settling tank transfering material pump 12.
The bottom discharge mouth of scrapper thin film evaporator 2 is sequentially connected slag charge kettle 6 and slag case 13 by pipeline, wherein, slag
Expect that kettle 6 includes cylinder, chuck and agitating device located at cylinder body outer wall, agitating device includes the motor in the middle part of cylinder top
With the puddler located at inner barrel；Exhaust outlet 14 is provided with the top side of slag case 13, exhaust outlet 14 connects tail gas absorption
Device, it can avoid polluting environment.The gas outlet of first gas-liquid separator 11 is sequentially connected the first surge tank 15, first by pipeline
Vavuum pump 16, the first pans 17 and the 3rd heat exchanger 18.
Slag charge kettle 6 is sequentially connected the 4th heat exchanger 19, the second gas-liquid separator 20, the second surge tank 21, by pipeline
Two vavuum pumps 22, the second pans 23 and the 5th heat exchanger 24.Second gas-liquid separator 20 is sequentially connected the 3rd by pipeline and connect
By tank 25 and middle transfering material pump 26.
O-dichlorohenzene mother liquor tank 1, to apply mechanically o-dichlorohenzene tank 4 and the quantity of slag charge kettle 6 be two, and two are used alternatingly.
Embodiment
Referring to Fig. 1, the present embodiment after the ring-closure reaction of permanent violet production process, will material mother liquor collect after replace into
Enter in o-dichlorohenzene mother liquor tank 1 or standby o-dichlorohenzene mother liquor tank 27, a tank can be collected first to full, the 3rd heat exchanger 18 of unlatching
Disengaging cooling water valve, be then turned on the first vavuum pump 16.When the vacuum in whole Distallation systm reaches more than -0.09MPa
When, mother liquor tank transfering material pump 7 is opened, o-dichlorohenzene mother liquor enters first according to the situation of vapo(u)rization system by the control of flowmeter 9
In heat exchanger 8, mother liquor is by First Heat Exchanger 8 and after evaporating into the gas phase heat exchange of First Heat Exchanger 8, into scraper plate film
Evaporator 2.
Now the motor of scrapper thin film evaporator 2 has been switched on, and the chuck conduction oil disengaging of scraper plate has been switched on, in scraper plate
Adjusted to 145 DEG C of temperature, mother liquor temperature after preheating enters scraper plate at 55 ~ 65 DEG C, rotated by scraper plate, after preheating
Mother liquor formed wall stream, at high temperature, gasification enter rectifying column 3, effect of the o-dichlorohenzene in the filler and distributor of rectifying column 3
Under, the gas-liquid in formation system is exchanged, and separates the o-dichlorohenzene gas phase after rectifying and enters First Heat Exchanger 8, and heat is carried out with mother liquor
Exchange.
Gas phase o-dichlorohenzene is after First Heat Exchanger 8, into the second heat exchanger 10 for having been switched on cooling water disengaging valve
In, after secondary cooling, the temperature for distilling out o-dichlorohenzene is reduced to 30 ~ 35 DEG C, flows into the first gas-liquid separator 11, then flow into certainly
Enter to apply mechanically o-dichlorohenzene tank 4 or it is standby apply mechanically o-dichlorohenzene tank 28, apply mechanically tank for two and be used alternatingly, one it is full after overflow water enter
Settling tank 5, is observed by visor, and after overflow is anhydrous, the o-dichlorohenzene gravity flow in the first gas-liquid separator 11 switches to standby set
With o-dichlorohenzene tank 28.The o-dichlorohenzene tank 4 of applying mechanically for filling o-dichlorohenzene is opened and applies mechanically o-dichlorohenzene tank transfering material pump 29 accordingly
Applied mechanically into workshop.After reaching certain liquid level in settling tank 5, settling tank transfering material pump 12 is opened, bottom will be deposited in
O-dichlorohenzene, which is transferred to, to be applied mechanically o-dichlorohenzene tank 4 or standby applies mechanically in o-dichlorohenzene tank 28.
After distillation removes 88% ~ 93% o-dichlorohenzene in scraper plate film, raffinate has certain fluidity, and raffinate flows into certainly
Enter slag charge kettle 6 or standby slag charge kettle 30, two slag charge kettles are used alternatingly.After raffinate entrance occurs in the slag charge kettle 6 begun to use, open
The disengaging valve of thermal conductivity deep fat is opened, opens the second vavuum pump 22 of 6 corresponding vacuum system of slag charge kettle, by remnants o-dichlorohenzene
Steam and the second corresponding gas-liquid separator 20 is flowed into by respective 4th heat exchanger 19, from corresponding 3rd pans of inflow
25, enter after the 3rd pans 25 are full by middle transfering material pump 26 and apply mechanically o-dichlorohenzene tank 4.
Raffinate in slag charge kettle 6 is constantly supplemented by scrapper thin film evaporator 2, and temperature is more constant initial stage, is 152 DEG C,
When material reaches kettle appearance half in kettle, switching slag charge kettle 6 causes raffinate to enter standby slag charge kettle 29.There is the slag charge of half kettle slag charge
The raffinate of kettle 6 is after distillation, and temperature is stepped up to 185 DEG C in slag charge kettle 6, now closes vacuum, opens the bottom valve of slag charge kettle 6,
Waste residue is put into slag case 13, slagging waste gas enters device for absorbing tail gas.
Scraper plate film continuous still mode is incorporated in permanent violet o-dichlorohenzene mother liquor by distilling apparatus of the present utility model
It is distilled to recover so that the distillation of o-dichlorohenzene mother liquor realizes serialization, scale；Its technological operation is simple, takes up an area less, recovery
Efficiency high, energy consumption are low, and the temperature deformation of equipment is less, and maintenance of equipment rate is low；Scraper plate thin film evaporation realizes raising recovery neighbour two
The effect of chlorobenzene content, more than 97.8% is brought up to from the 96.5% of common unit distillation content, for stable permanent violet pigment
Production technology is laid a good foundation.
In description of the present utility model, it is to be understood that term " " center ", " longitudinal direction ", " transverse direction ", " on ", " under ",
The orientation or position relationship of the instruction such as "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom ", " interior ", " outer " are
Based on orientation shown in the drawings or position relationship, it is for only for ease of description the utility model and simplifies description, rather than instruction
Or imply that signified device or element must have specific orientation, with specific azimuth configuration and operation, therefore be not understood that
For to limitation of the present utility model.In addition, term " first ", " second " be only used for describe purpose, and it is not intended that instruction or
Imply relative importance.
, it is necessary to which explanation, unless otherwise clearly defined and limited, term " are pacified in description of the present utility model
Dress ", " connected ", " connection " should be interpreted broadly, for example, it may be fixedly connected or be detachably connected, or integratedly
Connection；Can be mechanical connection or electrical connection；Can be joined directly together, can also be indirectly connected by intermediary,
It can be the connection of two element internals.For the ordinary skill in the art, above-mentioned art can be understood with concrete condition
Concrete meaning of the language in the utility model.
General principle, principal character and advantage of the present utility model has been shown and described above.The technical staff of the industry
It should be appreciated that above-described embodiment does not limit the utility model in any form, it is all by the way of equivalent substitution or equivalent transformation
The technical scheme obtained, all falls within the scope of protection of the utility model.
Claims (8)
1. energy-saving type vacuum flash distillation device, it is characterised in that including o-dichlorohenzene mother liquor tank, scrapper thin film evaporator, essence
Evaporate tower, apply mechanically o-dichlorohenzene tank, settling tank and slag charge kettle, the o-dichlorohenzene mother liquor tank is sequentially connected mother liquor tank by pipeline and turned
Material pump, First Heat Exchanger, scrapper thin film evaporator and rectifying column, the gas outlet of the rectifying column are sequentially connected first by pipeline
Heat exchanger, the second heat exchanger, the first gas-liquid separator, o-dichlorohenzene tank and settling tank are applied mechanically, the scrapper thin film evaporator
Bottom discharge mouth is sequentially connected slag charge kettle and slag case by pipeline, the gas outlet of first gas-liquid separator by pipeline according to
The first surge tank of secondary connection, the first vavuum pump, the first pans and the 3rd heat exchanger.
2. the energy-saving type vacuum flash distillation device according to claim 1 slag case, it is characterised in that the mother liquor tank turns
Flowmeter is additionally provided between material pump and First Heat Exchanger.
3. the energy-saving type vacuum flash distillation device according to claim 1 slag case, it is characterised in that the settling tank
Bottom side is provided with discharging opening, and the discharging opening applies mechanically o-dichlorohenzene tank by the connection of settling tank transfering material pump.
4. the energy-saving type vacuum flash distillation device according to claim 1 slag case, it is characterised in that the slag case
Top side is provided with exhaust outlet, and the exhaust outlet connects device for absorbing tail gas.
5. the energy-saving type vacuum flash distillation device according to claim 1 slag case, it is characterised in that the slag charge kettle leads to
Piping is sequentially connected the 4th heat exchanger, the second gas-liquid separator, the second surge tank, the second vavuum pump, the second pans and
Five heat exchangers.
6. the energy-saving type vacuum flash distillation device according to claim 5 slag case, it is characterised in that second gas-liquid
Separator is sequentially connected the 3rd pans and middle transfering material pump by pipeline.
7. the energy-saving type vacuum flash distillation device according to claim 1 slag case, it is characterised in that the slag charge kettle bag
Include cylinder, chuck and agitating device located at cylinder body outer wall, the agitating device include motor in the middle part of cylinder top and
Located at the puddler of inner barrel.
8. the energy-saving type vacuum flash distillation device according to claim 1 slag case, it is characterised in that the o-dichlorohenzene
Mother liquor tank, to apply mechanically o-dichlorohenzene tank and the quantity of slag charge kettle be two, and two are used alternatingly.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720149182.8U CN206631232U (en) | 2017-02-20 | 2017-02-20 | Energy-saving type vacuum flash distillation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720149182.8U CN206631232U (en) | 2017-02-20 | 2017-02-20 | Energy-saving type vacuum flash distillation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206631232U true CN206631232U (en) | 2017-11-14 |
Family
ID=60252384
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720149182.8U Expired - Fee Related CN206631232U (en) | 2017-02-20 | 2017-02-20 | Energy-saving type vacuum flash distillation device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206631232U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111848338A (en) * | 2020-08-27 | 2020-10-30 | 银川百泓新材料科技有限公司 | Method and device for recovering o-dichlorobenzene from permanent violet centrifugal mother liquor |
| CN111849192A (en) * | 2020-08-31 | 2020-10-30 | 银川百泓新材料科技有限公司 | Permanent purple centrifugal mother liquor processing system |
-
2017
- 2017-02-20 CN CN201720149182.8U patent/CN206631232U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111848338A (en) * | 2020-08-27 | 2020-10-30 | 银川百泓新材料科技有限公司 | Method and device for recovering o-dichlorobenzene from permanent violet centrifugal mother liquor |
| CN111848338B (en) * | 2020-08-27 | 2023-12-22 | 银川百泓新材料科技有限公司 | Method and device for recovering o-dichlorobenzene from permanent violet centrifugal mother liquor |
| CN111849192A (en) * | 2020-08-31 | 2020-10-30 | 银川百泓新材料科技有限公司 | Permanent purple centrifugal mother liquor processing system |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20171114 Termination date: 20200220 |