CN208802952U - A kind of vacuum distillation dephenolize equipment - Google Patents
A kind of vacuum distillation dephenolize equipment Download PDFInfo
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- CN208802952U CN208802952U CN201821262841.XU CN201821262841U CN208802952U CN 208802952 U CN208802952 U CN 208802952U CN 201821262841 U CN201821262841 U CN 201821262841U CN 208802952 U CN208802952 U CN 208802952U
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- Prior art keywords
- pipeline
- extraction
- outlet
- heat exchanger
- tower
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- 238000005292 vacuum distillation Methods 0.000 title claims abstract description 21
- 238000000605 extraction Methods 0.000 claims abstract description 71
- 239000002351 wastewater Substances 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000000203 mixture Substances 0.000 claims description 9
- 150000002989 phenols Chemical class 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 5
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 2
- 238000004821 distillation Methods 0.000 claims 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 abstract description 32
- 238000010438 heat treatment Methods 0.000 abstract description 7
- 238000000034 method Methods 0.000 abstract description 7
- 235000013824 polyphenols Nutrition 0.000 abstract description 6
- 238000000926 separation method Methods 0.000 abstract description 4
- 150000008442 polyphenolic compounds Chemical class 0.000 abstract description 2
- 238000006731 degradation reaction Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 7
- 239000000284 extract Substances 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- DCKVNWZUADLDEH-UHFFFAOYSA-N sec-butyl acetate Chemical compound CCC(C)OC(C)=O DCKVNWZUADLDEH-UHFFFAOYSA-N 0.000 description 2
- 238000002834 transmittance Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009395 breeding Methods 0.000 description 1
- 230000001488 breeding effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000003809 water extraction Methods 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses the utility model to devise a kind of vacuum distillation dephenolize equipment, including destilling tower, vacuum pump, extraction tower, First Heat Exchanger, stripper, oil water separator, holding vessel, second heat exchanger and rectifying column, the dephenolizing process includes: first step vacuum distillation, the extraction of second step waste water, third step raffinate phase stripping and the 4th step resource reclaim, the High-Efficiency Phenol-Degradation of phenol wastewater is realized by aforementioned four step, this programme carries out steam dephenolize to phenol wastewater by way of vacuum distillation, reduce the bubble point of phenol wastewater, to reduce separation temperature, reduce steam consumption for heating, reextraction dephenolize is carried out to the waste water of steam dephenolize, the two combines, compensate for the lower disadvantage of extracting and dephenolizing polyphenol extraction yield, greatly refer to the extraction yield of Phenol for Waste Water, reduce the pollution to environment.
Description
Technical field
The utility model relates to dephenolize technical field, specially a kind of vacuum distillation dephenolize equipment.
Background technique
Phenol wastewater is the waste water containing phenolic substances, from a wealth of sources, and harm is larger, and phenol wastewater is discharged into without processing
Water body can endanger the breeding and existence of aquatile.
Existing phenolic wastewater treatment mode, including steam dephenolize and extracting and dephenolizing etc., wherein phenol is recycled in steam dephenolize
Quality is higher, but steam consumption is big, and remaining phenol content is higher in waste water, and extracting and dephenolizing is existing main dephenolize means,
Extracting and dephenolizing application extractant carries out dephenolize, and the wide variety of extractant, benzene kind of extractants dephenolize efficiency is lower, but price is just
Preferably, ether-ether kind of extractants dephenolize efficiency is higher, but it is water-soluble stronger, is not easy to recycle, and price is higher, while most
Extractant is relatively low to the extraction effect of polyphenol, and to solve the above-mentioned problems, we have proposed a kind of vacuum distillation dephenolizes to set
It is standby.
Utility model content
The purpose of this utility model is to provide a kind of vacuum distillation dephenolize equipment, to solve to propose in above-mentioned background technique
The problem of.
To achieve the above object, the utility model provides the following technical solutions: a kind of vacuum distillation dephenolize equipment, including steams
Evaporate tower, vacuum pump, extraction tower, First Heat Exchanger, stripper, oil water separator, holding vessel, the second heat exchanger and rectifying column, institute
It states destilling tower and is connected by pipeline with vacuum pump, the upper end of the destilling tower offers feed(raw material)inlet and gas vent, described
The lower end of destilling tower offers wastewater outlet, and the upper end of the extraction tower offers waterwater entrance and extraction phase outlet, described useless
Water inlet is connected by pipeline with wastewater outlet, and the lower end of the extraction tower offers raffinate phase outlet, and the raffinate phase goes out
Mouth is connected by pipeline with stripper, and the upper end of the stripper offers azeotropic mixture outlet, and the lower end of the stripper is opened
Equipped with outlet of sewer, the right side wall fixing assembling of the stripper has oil water separator, and oil water separator passes through pipeline together
The outlet of boiling object is connected, and the output end of the oil water separator is connected by pipeline with stripper, and the oil water separator is logical
Piping is connected with holding vessel input terminal, and the output end of the holding vessel is connected by pipeline with extraction tower, the storage
The upper end of tank offers extractant entrance, and the holding vessel is connected by pipeline with rectifying column, offers on the rectifying column
Extraction phase entrance, the extraction phase entrance are connected by pipeline with extraction phase outlet, and the lower end of the rectifying column offers slightly
Phenol outlet.
Preferably, the raffinate phase outlet is connected by pipeline with the first input end of First Heat Exchanger, and described first
First output end of heat exchanger is connected by pipeline with stripper, and the lower end of the outlet of sewer passes through pipeline and the first heat exchange
Second input terminal of device is connected, and the second output terminal of the First Heat Exchanger is communicated with pipeline.
Preferably, the holding vessel is connected by pipeline with the first input end of the second heat exchanger, second heat exchange
First output end of device is connected by pipeline with rectifying column, and the extraction phase entrance passes through the second of pipeline and the second heat exchanger
Input terminal is connected, and the second output terminal of second heat exchanger is connected by pipeline with extraction phase outlet.
Compared with prior art, the utility model has the beneficial effects that a kind of vacuum distillation dephenolize equipment, this programme pass through
The mode of vacuum distillation carries out steam dephenolize to phenol wastewater, reduces the bubble point of phenol wastewater, to reduce separation temperature, reduces
Steam consumption for heating carries out reextraction dephenolize to the waste water of steam dephenolize, and the two combines, and it is more to compensate for extracting and dephenolizing
The lower disadvantage of first phenol extraction rate greatly refers to the extraction yield of Phenol for Waste Water, reduces the pollution to environment.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of this patent.
In figure: 1 destilling tower, 11 feed(raw material)inlets, 12 gas vents, 13 wastewater outlets, 2 vacuum pumps, 3 extraction towers, 31 waste water
Entrance, the outlet of 32 extraction phases, the outlet of 33 raffinate phases, the outlet of 4 First Heat Exchangers, 5 strippers, 51 azeotropic mixtures, 52 outlets of sewer, 6
Oil water separator, 7 holding vessels, 71 extractant entrances, 8 second heat exchangers, 9 rectifying columns, 91 extraction phase entrances, the outlet of 92 crude phenols.
Specific embodiment
The utility model is described further below in conjunction with specific embodiment, but the protection scope of the utility model
It is not limited to this.
Referring to Fig. 1, the utility model provides a kind of technical solution: a kind of vacuum distillation dephenolize equipment, including destilling tower
1, vacuum pump 2, extraction tower 3, First Heat Exchanger 4, stripper 5, oil water separator 6, holding vessel 7, the second heat exchanger 8 and rectifying column
9, destilling tower 1 is connected by pipeline with vacuum pump 2, and the upper end of destilling tower 1 offers feed(raw material)inlet 11 and gas vent 12,
The lower end of destilling tower 1 offers wastewater outlet 13, and the upper end of extraction tower 3 offers waterwater entrance 31 and extraction phase outlet 32, gives up
Water inlet 31 is connected by pipeline with wastewater outlet 13, and the lower end of extraction tower 3 offers raffinate phase outlet 33, raffinate phase outlet
33 are connected by pipeline with stripper 5, and the upper end of stripper 5 offers azeotropic mixture outlet 51, and the lower end of stripper 5 offers
Outlet of sewer 52, the right side wall fixing assembling of stripper 5 has oil water separator 6, and oil water separator 6 passes through pipeline and azeotropic mixture
Outlet 51 is connected, and the output end of oil water separator 6 is connected by pipeline with stripper 5, and oil water separator 6 passes through pipeline
It is connected with 7 input terminal of holding vessel, the output end of holding vessel 7 is connected by pipeline with extraction tower 3, and the upper end of holding vessel 7 is opened
Equipped with extractant entrance 71, holding vessel 7 is connected by pipeline with rectifying column 9, and extraction phase entrance 91 is offered on rectifying column 9,
Extraction phase entrance 91 is connected by pipeline with extraction phase outlet 32, and the lower end of rectifying column 9 offers crude phenols outlet 92.
Raffinate phase outlet 33 is connected by pipeline with the first input end of First Heat Exchanger 4, and the first of First Heat Exchanger 4
Output end is connected by pipeline with stripper 5, and it is second defeated to pass through pipeline and First Heat Exchanger 4 for the lower end of outlet of sewer 52
Enter end to be connected, the second output terminal of First Heat Exchanger 4 is communicated with pipeline.
The present apparatus changes the raffinate phase output channel of extraction tower 3 and 52 lower channel of outlet of sewer of stripper 5
Heat, the waste heat that the discharge sewage of outlet of sewer 52 is utilized preheat the raffinate phase in raffinate phase output channel, reduce heating
The energy of raffinate phase consumption.
Holding vessel 7 is connected by pipeline with the first input end of the second heat exchanger 8, the first output of the second heat exchanger 8
End is connected by pipeline with rectifying column 9, and extraction phase entrance 91 is connected by pipeline with the second input terminal of the second heat exchanger 8
Logical, the second output terminal of the second heat exchanger 8 is connected by pipeline with extraction phase outlet 32.
The extraction phase output channel of extraction tower 3 is connected to holding vessel 7 with 9 tower top of rectifying column and carries out extractant recycling by the present apparatus
Pipeline exchange heat, the waste heat that the extractant of recycling is utilized preheats the extraction phase in extraction phase output channel, subtracts
The energy of heating extraction phase consumption less.
First Heat Exchanger 4 and the second heat exchanger 8 are tubular heat exchanger, and a kind of fluid is entered by the connecting piece of end socket,
In Guan Liudong, flowed out from the outlet of the end socket other end, this is referred to as tube side；One other fluid is entered by the adapter tube of shell, from shell
It is flowed out at another adapter tube on body, this is known as shell side, and fluid will not contact mixing with fluid in shell side in tube side, and mutually carry out
Heat exchange.
First Heat Exchanger 4 and first input end in the second heat exchanger 8 and the first output end are tube side in the present embodiment, the
Two input terminals and second output terminal are shell side.
Vacuum distillation dephenolizing process includes: S1. vacuum distillation, the extraction of S2. waste water, S3. raffinate phase stripping, S4. resource time
It receives, this four steps constitute vacuum distillation dephenolizing process.
The first step, vacuum distillation specifically: phenolic waste liquor is put into destilling tower 1 from feed(raw material)inlet 11, opens vacuum
Pump 2 persistently extracts the interior gases of destilling tower 1, forms negative pressure in destilling tower 1, destilling tower 1 under negative pressure state to phenolic waste liquor into
Row vacuum distillation, the vapor containing phenol of generation, the vapor containing phenol are discharged from gas vent 12, are discharged to from gas vent 12
Vapor containing phenol be collected, the vapor containing phenol of collection is imported in lye and is washed, the phenol in vapor containing phenol is recycled.
Vacuum pump 2 continues working, and maintains the state of negative pressure in destilling tower 1, the mode of vacuum distillation to phenol wastewater into
Row steam dephenolize, reduces the bubble point of phenol wastewater, to reduce separation temperature, reduces steam consumption for heating.
Pipeline between present apparatus wastewater outlet 13 and waterwater entrance 31, extraction phase outlet 32 and extraction phase entrance 91 it
Between pipeline, be mounted on circulation on the pipeline between pipeline and holding vessel 7 and rectifying column 9 between extraction tower 3 and holding vessel 7
Pump, circulating pump connect external power supply, are controlled by switch, the liquid in circulating pump subsidiary conduit is flowed.
Second step, waste water extraction specifically: preliminary dephenolize waste water passes through pipeline and waste water from wastewater outlet 13 in destilling tower 1
Entrance 31 flows into extraction tower 3, and extract liquor enters 3 tower bottom of extraction tower, preliminary dephenolize waste water by pipeline out of holding vessel 7
It is extracted after being mixed with extract liquor, the extraction phase generated after extraction passes through pipeline and extraction from the extraction phase on 3 top of extraction tower outlet 32
It takes phase entrance 91 to be flowed into rectifying column 9, is exchanged heat in extraction phase transmittance process by the second heat exchanger 8, generated after extraction
Raffinate phase 33 be flowed into stripper 5 by pipeline from the outlet of the raffinate phase of 3 bottom end of extraction tower, it is logical in raffinate phase transmittance process
First Heat Exchanger 4 is crossed to exchange heat.
Third step, raffinate phase stripping specifically: raffinate phase is heated after entering in stripper 5, the raffinate after heating
The azeotropic mixture that extractant and water in phase are formed flows into oil water separator 6, oil water separator by pipeline from azeotropic mixture outlet 51
Water phase after 6 separation is flowed back into stripper 5 by pipeline, and the isolated extractant of oil water separator 6 is flowed by pipeline and stored up
It stores in tank 7, the waste water in stripper 5 is discharged by outlet of sewer 52, is carried out at biochemistry to the waste water that outlet of sewer 52 is discharged
Reason.
4th step, resource reclaim specifically: extraction phase enters and carries out rectifying in rectifying column 9, extracts after rectifying in rectifying column 9
The extractant in phase is taken to be flowed into holding vessel 7 by pipeline, the remaining coarse powder product in 9 bottom of rectifying column exports 92 from crude phenols
Discharge, realizes secondary dephenolize.
Extractant used is specially sec-butyl acetate in the extraction of second step waste water, and extractant pH value is 8, extraction temperature 40
~45 degrees Celsius, the sec-butyl acetate extractant under above-mentioned environment is preferable to the dephenolization effect of waste water, improves dephenolize rate.
Working principle: the present apparatus include destilling tower, vacuum pump, extraction tower, First Heat Exchanger, stripper, oil water separator,
Holding vessel, the second heat exchanger and rectifying column realize the phenol removal to phenol wastewater using the assembling cooperation of these devices, first
Phenol wastewater is passed into destilling tower 1 and is distilled, the vapor containing phenol of discharge is collected from gas vent 12, containing for collection
Phenol vapor is imported in lye and is washed, and recycles the phenol in vapor containing phenol, and preliminary dephenolize waste water is discharged into extraction from wastewater outlet 13
It is extracted in tower 3, the extraction phase generated after extraction is drained into rectifying column 9 by extraction phase outlet 32, is generated after extraction
Raffinate phase is drained into stripper 5 by raffinate phase outlet 33, and raffinate phase is heated after entering in stripper 5, after heating
Raffinate phase in extractant and water formed azeotropic mixture from azeotropic mixture outlet 51 by pipeline inflow oil water separator 6, grease
Water phase after separator 6 separates is flowed back into stripper 5 by pipeline, and the isolated extractant of oil water separator 6 passes through pipeline
It flows into accumulator tank 7, realizes the recycling of extractant, the waste water in stripper 5 is discharged by outlet of sewer 52, to outlet of sewer 52
The waste water of discharge carries out biochemical treatment, and extraction phase enters and carries out rectifying in rectifying column 9, in rectifying column 9 after rectifying in extraction phase
Extractant be flowed into holding vessel 7 by pipeline, realize the recycling of extractant, the remaining coarse powder product in 9 bottom of rectifying column from
92 discharge of crude phenols outlet, realizes secondary dephenolize, crude phenols are recycled.
Claims (3)
1. a kind of vacuum distillation dephenolize equipment, it is characterised in that: including destilling tower (1), vacuum pump (2), extraction tower (3), first
Heat exchanger (4), stripper (5), oil water separator (6), holding vessel (7), the second heat exchanger (8) and rectifying column (9), the distillation
Tower (1) is connected by pipeline with vacuum pump (2), and the upper end of the destilling tower (1) offers feed(raw material)inlet (11) and gas goes out
Mouth (12), the lower end of the destilling tower (1) offer wastewater outlet (13), and the upper end of the extraction tower (3) offers waste water and enters
Mouth (31) and extraction phase outlet (32), the waterwater entrance (31) are connected by pipeline with wastewater outlet (13), the extraction
The lower end of tower (3) offers raffinate phase outlet (33), and the raffinate phase outlet (33) is connected by pipeline with stripper (5),
The upper end of the stripper (5) offers azeotropic mixture outlet (51), and the lower end of the stripper (5) offers outlet of sewer
(52), the right side wall fixing assembling of the stripper (5) has oil water separator (6), and oil water separator (6) passes through pipeline together
Boiling object outlet (51) is connected, and the output end of the oil water separator (6) is connected by pipeline with stripper (5), the oil
Separator (6) is connected by pipeline with holding vessel (7) input terminal, and the output end of the holding vessel (7) passes through pipeline and extraction
Take tower (3) to be connected, the upper end of the holding vessel (7) offers extractant entrance (71), the holding vessel (7) by pipeline with
Rectifying column (9) is connected, and offers extraction phase entrance (91) on the rectifying column (9), and the extraction phase entrance (91) passes through pipe
Road is connected with extraction phase outlet (32), and the lower end of the rectifying column (9) offers crude phenols outlet (92).
2. a kind of vacuum distillation dephenolize equipment according to claim 1, it is characterised in that: the raffinate phase outlet (33) is logical
Piping is connected with the first input end of First Heat Exchanger (4), and the first output end of the First Heat Exchanger (4) passes through pipeline
It is connected with stripper (5), the lower end of the outlet of sewer (52) passes through the second input terminal phase of pipeline and First Heat Exchanger (4)
Connection, the second output terminal of the First Heat Exchanger (4) are communicated with pipeline.
3. a kind of vacuum distillation dephenolize equipment according to claim 1, it is characterised in that: the holding vessel (7) passes through pipe
Road is connected with the first input end of the second heat exchanger (8), and the first output end of second heat exchanger (8) passes through pipeline and essence
It evaporates tower (9) to be connected, the extraction phase entrance (91) is connected by pipeline with the second input terminal of the second heat exchanger (8), institute
The second output terminal for stating the second heat exchanger (8) is connected by pipeline with extraction phase outlet (32).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821262841.XU CN208802952U (en) | 2018-08-07 | 2018-08-07 | A kind of vacuum distillation dephenolize equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821262841.XU CN208802952U (en) | 2018-08-07 | 2018-08-07 | A kind of vacuum distillation dephenolize equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208802952U true CN208802952U (en) | 2019-04-30 |
Family
ID=66231310
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201821262841.XU Expired - Fee Related CN208802952U (en) | 2018-08-07 | 2018-08-07 | A kind of vacuum distillation dephenolize equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208802952U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110818156A (en) * | 2018-08-07 | 2020-02-21 | 唐山祥旭环保科技有限公司 | Negative pressure distillation dephenolization equipment and dephenolization process thereof |
| CN111547913A (en) * | 2019-12-16 | 2020-08-18 | 昆山美淼环保科技有限公司 | Method for recovering phenol from phenol-containing wastewater |
-
2018
- 2018-08-07 CN CN201821262841.XU patent/CN208802952U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110818156A (en) * | 2018-08-07 | 2020-02-21 | 唐山祥旭环保科技有限公司 | Negative pressure distillation dephenolization equipment and dephenolization process thereof |
| CN111547913A (en) * | 2019-12-16 | 2020-08-18 | 昆山美淼环保科技有限公司 | Method for recovering phenol from phenol-containing wastewater |
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| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20190430 |