CN207130213U - A kind of tar cooling and distilling apparatus - Google Patents
A kind of tar cooling and distilling apparatus Download PDFInfo
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- CN207130213U CN207130213U CN201720818520.2U CN201720818520U CN207130213U CN 207130213 U CN207130213 U CN 207130213U CN 201720818520 U CN201720818520 U CN 201720818520U CN 207130213 U CN207130213 U CN 207130213U
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- Prior art keywords
- tar
- oil
- tower
- carbon black
- tube furnace
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Abstract
The utility model discloses a kind of cooling of tar and distilling apparatus, including dehydration workshop section and distillation workshop section, dehydration workshop section is connected in sequence by feed preheater, washing oil condensate cooler, two contaminated product heat exchangers, mixed triolein condenser, flash oil condensing device and dehydrating tower；The distillation workshop section includes tube furnace, tar/carbon black oil heat exchanger and cut tower.The apparatus system of this practical information, during operation raw material heating and finished product cooling mainly exchanged heat and diamond heating is got using raw material and finished product are multiple, without superheated steam heating；Technological process is short, the heat exchange increase of raw material finished product, and energy consumption is low, stable operation, product quality are high, energy utilization rate is high, not only saves labour, and production is more intensive, and cleaning ambient, while accurate control feeding amount, can effectively improve production efficiency.
Description
Technical field
It the utility model is related to transformation to set and coal tar deep processing technical field, and in particular to a kind of to save the energy
Tar cools down and distilling apparatus.
Background technology
Coal tar is the byproduct in process of coking, is condensed by coke-oven gas.Coal tar production, which generally requires, to be passed through
Distillation is divided into light oil, carbolic oil, naphtalene oil, washing oil, carbolineum and pitch, then carries out deep processing.Typical tar continuous still work
Skill has air-distillation, vacuum distillation and atmospheric and vacuum distillation.
Coal tar distillation is not added with alkali, serious corrosion can be produced in still-process, but the traditional handicraft added and subtracted can be led again
Cause product quality low.Have research by improve Distallation systm equipment and pipe material, control normal operating and shutting down mode and
Parameter etc., caused corrosion impact is not added and subtracted to overcome, there is certain good effect.But needed in whole process substantial amounts of
Thermal source, such as king-tower bottom need circulation, the bottom of asphalt tower in heating furnace progress to be also required to circulate by setting in heating furnace
Deng.
Utility model content
To solve above mentioned problem of the prior art, the utility model provides a kind of tar cooling and distilling apparatus, fitted
The tar distillation process that coal tar distillation is not added with alkali, double tower list stove heat Atmospheric vacuum combines is closed, is effectively increased to the energy
Saving and recycling to heat.
Tar cooling provided by the utility model and distilling apparatus, including dehydration workshop section and distillation workshop section, the dehydration work
Section is by feed preheater, washing oil condensate cooler, two contaminated product heat exchangers, mixed triolein condenser, flash oil condensing device and dehydrating tower
It is connected in sequence；The distillation workshop section includes tube furnace, tar/carbon black oil heat exchanger and cut tower；
The outlet at bottom line branching of dehydrating tower connects the arrival end and pipe of tar/carbon black oil heat exchanger respectively into two
The entrance of formula stove；
Tar/carbon black oil heat exchanger is connected to dehydrating tower provided with outlet；
The entrance of the outlet conduit connection cut tower of tube furnace；
Cut tower bottom is provided with export pipeline, is branched off into two and is respectively connecting to tar/carbon black oil heat exchanger and tube furnace,
Convection section, which is formed, into the pipeline in tube furnace passes tube furnace connection cut tower again；
On the pipeline between pipeline, dehydrating tower and tube furnace between the dehydrating tower and tar/carbon black oil heat exchanger
Provided with circulating pump.
Said apparatus, raw material heating and finished product cooling are mainly obtained using raw material heat exchange multiple with finished product and diamond heating
Come, heated without superheated steam, greatly save thermal energy consumption.
Preferably, radiant section is additionally provided with the tube furnace to be used to heat maltha.The maltha warp of cut bottom of towe extraction
It can be cut tower circulating-heating to cross and return to cut tower after heating, and cut tower can save its special heating furnace heat supply.
Preferably, dehydrating tower is also connected with light oil cooler and oil water separator, and light oil backflash is provided with light oil cooler；
Light oil backflash one end is connected to dehydrating tower, and edible vegetable oil medial launder is connected at the top of light oil backflash.Light oil gas passes through at the top of dehydrating tower
Light oil cooler and oil water separator, the aqueous phase that oil water separator is separated flow to a phenol tank certainly.Light oil enters backflash,
A part is back to dehydrating tower, and unnecessary light oil enters light oil medial launder by backflash flowing full.
Preferably, fraction overhead portion is connected to washing oil condensate cooler provided with pipeline.Fraction overhead produces mixed fraction, leads to
Piping is transported to washing oil condensate cooler and carries out cooling heat transferring.
Preferably, be additionally provided with washing oil backflash between washing oil condensate cooler and mixed triolein cooler, washing oil backflash with
The return duct with reflux pump is additionally provided between cut tower.
The phenol naphthalene of fraction overhead effusion washes mixed oil and gas after washing oil condensate cooler partial condensation, and it is cold that liquid phase enters washing oil
Solidifying cooler, after gas phase enters the heat exchange of two contaminated product heat exchangers, liquid phase enters mixed triolein condenser, and gas phase portion can not coagulate by one
Enter vacuum system after Gas Cooler cooling.The washing oil come out from washing oil condensate cooler enters washing oil backflash, and a part is washed
Oil distillate sends fraction overhead back to by backflow of the reflux pump as cut tower, and remaining washing oil is sent to after mixed triolein condenser and do not washed
Mixing divides groove.
Preferably, fraction overhead portion is additionally provided with a vavuum pump.Vavuum pump is used to make cut tower keep negative pressure state.
Preferably, tar/carbon black oil heat exchanger connection carbon black oil pan tank.Carbon black oil pan tank be used for collect by tar/
The carbon black oil that carbon black oil heat exchanger comes out.
Compared with prior art, the utility model has the advantages that：
Device of the present utility model, enter after making raw tar heated in the middle part of dehydrating tower, dehydration column overhead extraction light oil
And water, then dehydrating tower bottom is heated through tube furnace convection section enters cut tower, fraction overhead extraction mixed fraction, bottom of towe extraction charcoal
A dirty oil part is heated back to cut tower by tube furnace radiant section and provides heat.Dehydrating tower origin of heat is essentially from dehydrating tower
Bottom returns to dehydrating tower with carbon black oil heat exchange and provides heat, and tar stock after semi-finished product, the multiple heat exchange of finished product by with absorbing heat.
The utility model not only saves labour, and production is more intensive, and cleaning ambient, while accurate control feeding amount, energy
Enough effectively improve production efficiency.
Brief description of the drawings
Tar cooling and distilling apparatus structural representation in Fig. 1 embodiments of the present utility model.
In figure：1 tar stock, 2 feed preheaters, 3 washing oil condensate coolers, 4 liang of contaminated product heat exchangers, the condensation of 5 mixed trioleins
Device, 6 flash oil condensing devices, 7 dehydrating towers, 8/9 tar/carbon black oil heat exchanger, 10 tube furnaces, 11 cut towers, 12 carbon black oils, 13 is soft
Pitch, 14 vavuum pumps, 15 washing oil, 16 naphthols mixed fractions, 17 naphthols wash mixed fraction.
Embodiment
In order that those skilled in the art more fully understand the utility model, with reference to embodiment pair
The utility model is described in further detail.
Referring to accompanying drawing 1, a kind of cooling of tar and distilling apparatus that the present embodiment is enumerated, including dehydration workshop section and distillation work
Section, the dehydration workshop section is by feed preheater 2, washing oil condensate cooler 34, two contaminated product heat exchangers, mixed triolein condenser 5, flash distillation
Oil condenser 6 and dehydrating tower 7 are connected in sequence；The distillation workshop section includes tube furnace 10, tar/carbon black oil heat exchanger 8/9
And cut tower 11.
The outlet at bottom line branching of dehydrating tower 7 connects the arrival end of tar/carbon black oil heat exchanger 8/9 respectively into two
With the entrance of tube furnace 10.Dehydrating tower 7 is also connected with light oil cooler (not shown) and oil water separator (not shown),
Light oil backflash is provided with light oil cooler；Light oil backflash one end is connected to dehydrating tower 7, and edible vegetable oil is connected at the top of light oil backflash
Medial launder.
Tar/carbon black oil heat exchanger 8/9 is connected to dehydrating tower 7 provided with outlet again；The outlet conduit connection of tube furnace 10 evaporates
Divide the entrance of tower 11.
The pipe between pipeline, dehydrating tower 7 and tube furnace 10 between the dehydrating tower 7 and tar/carbon black oil heat exchanger 8/9
Circulating pump is equipped with road.
The top of cut tower 11 is connected to washing oil condensate cooler 3 provided with pipeline, and the top of cut tower 11 is also connected with a vavuum pump
14.The bottom of cut tower 11 is provided with export pipeline, is branched off into two and is respectively connecting to tar/carbon black oil heat exchanger 8/9 and tube furnace
10, form convection section into the pipeline in tube furnace 10 and pass the connection cut of tube furnace 10 tower 11 again.It is additionally provided with tube furnace 10
Radiant section is used to heat maltha 13.
Washing oil backflash, washing oil backflash and cut tower are additionally provided between washing oil condensate cooler 3 and mixed triolein cooler 5
Between be additionally provided with the return duct with reflux pump.
The phenol naphthalene of the top of cut tower 11 effusion washes mixed oil and gas after washing oil condensate cooler partial condensation, and liquid phase enters washing oil
Condensate cooler 3, after gas phase enters the heat exchange of two contaminated product heat exchangers 4, liquid phase enters mixed triolein condenser 5, and gas phase portion can pass through
Enter vacuum system after the cooling of one fixed gas cooler.
More particularly, the applicable technique of the present embodiment device is as follows：
(1) raw tar 1 directly condenses with feed preheater 2, washing oil respectively through tar stock pump from the suction of raw material oil depot
Cooler 3, two contaminated product heat exchangers 4, mixed triolein condenser 5 and flash oil condensing device 6 enter the middle part of dehydrating tower 7 after heating.Dehydration
Tower tar inlet temperature：200~230 DEG C.
(2) 98~110 DEG C of tower top temperature is dehydrated, the light oil distillate and water of tower top effusion are cooled to 40 DEG C through light oil cooler
Afterwards, oil water separator is flowed into, light oil is separated from water.By light oil backflash, a part returns to dehydrating tower 7 and made the light oil isolated
For backflow, remaining light oil enters light oil medial launder as product by light oil backflash flowing full；The water separated flows into one certainly
Phenol tank.
The bottom of dehydrating tower 7 anhydrous tar (being dehydrated to less than 0.2%) part by anhydrous tar circulation be pumped to tar/
Carbon black oil heat exchanger 8/9, after tar/carbon black oil heat exchanger 8/9 exchanges heat, return dehydrating tower 7 and provide heat for it.Anhydrous Jiao
Oily another part is heated to 285 DEG C or so into convection section of the tube furnace 10 through tube furnace 10 and enters the progress negative pressure steaming of cut tower 11
Evaporate.
(3) the phenol naphthalene of the top of cut tower 11 effusion washes mixed oil and gas after the partial condensation of washing oil condensate cooler 3, and liquid phase stays in
Washing oil condensate cooler 3, after gas phase enters the heat exchange of two contaminated product heat exchangers 4, liquid phase enters mixed triolein condenser 5, gas phase portion warp
Enter vacuum system after the cooling of fixed gas cooler.The entrance washing oil backflash of washing oil 15 come out from washing oil condensate cooler 3, one
Part wash oil fraction sends fraction tower top back to by reflux pump as the backflow of cut tower, and remaining washing oil 15 is by mixed triolein condenser 5
After be sent to do not wash mixing part groove.
Washing oil condensate cooler 3 is exchanged heat by washing oil 15 in tar stock 1 and mixed fraction；Two contaminated product heat exchangers 4 are by tar
Naphthols mixed fraction 16 exchanges heat in raw material 1 and mixed fraction；Mixed triolein condenser 5 washes mixed fraction 17 and tar stock by naphthols
1 heat exchange；Flash oil condensing device 6 is exchanged heat by tar stock 1 and carbon black oil 12.Tar stock 1 after multiple heat exchange obtains abundance
Heat reach 200 DEG C or so enter dehydrating towers 7.
The carbon black oil that the bottom of cut tower 11 is isolated, through carbon black oil circulating pump, a part is sent to the radiant section of tube furnace 10 and added
The bottom of cut tower 11 is returned to after heat.A part is sent to tar/carbon black oil heat exchanger 8/9 with after tar heat exchange, isolating carbon black oil,
Introduce pan tank.
Each workshop section's important technological parameters are as follows：
Dehydrating tower tar inlet temperature：200~230 DEG C,
Tube furnace convection section outlet temperature：275~295 DEG C,
Tube furnace radiant section outlet temperature：320 ± 3 DEG C,
It is dehydrated tower top temperature：95~110 DEG C,
It is dehydrated column bottom temperature：240~260 DEG C,
Fraction overhead temperature：205~230 DEG C,
Cut column bottom temperature：290~300 DEG C,
It is dehydrated tower overhead gas phase pressure：0~10kPa,
Dehydrating tower spirit phase pressure：5~10kPa,
Fraction overhead gaseous pressure：- 40kPa,
Cut bottom of towe gaseous pressure：-30kPa.
Corresponding technique is coordinated using above-mentioned tar cooling of the present utility model and distilling apparatus, can realize that operating parameter is steady
Fixed, production capacity high yield quality is high；Energy regenerating utilization rate is high, many excellent effects such as energy consumption is low.
Specific case used herein is set forth to principle of the present utility model and embodiment, above example
Explanation be only intended to help and understand core concept of the present utility model.It should be pointed out that the ordinary skill for the art
For personnel, on the premise of the utility model principle is not departed from, some improvement and modification can also be carried out to the utility model,
These are improved and modification is also fallen into the protection domain of the utility model claims.
Claims (7)
1. a kind of cooling of tar and distilling apparatus, including dehydration workshop section and distillation workshop section, it is characterised in that the dehydration workshop section by
Feed preheater, washing oil condensate cooler, two contaminated product heat exchangers, mixed triolein condenser, flash oil condensing device and dehydrating tower are successively
It is formed by connecting；The distillation workshop section includes tube furnace, tar/carbon black oil heat exchanger and cut tower；
The outlet at bottom line branching of dehydrating tower connects the arrival end and tube furnace of tar/carbon black oil heat exchanger respectively into two
Entrance；
Tar/carbon black oil heat exchanger is connected to dehydrating tower provided with outlet；
The entrance of the outlet conduit connection cut tower of tube furnace；
Cut tower bottom is provided with export pipeline, is branched off into two and is respectively connecting to tar/carbon black oil heat exchanger and tube furnace, enters
Pipeline in tube furnace forms convection section and passes tube furnace connection cut tower again；
It is equipped with the pipeline between pipeline, dehydrating tower and tube furnace between the dehydrating tower and tar/carbon black oil heat exchanger
Circulating pump.
2. tar cooling according to claim 1 and distilling apparatus, it is characterised in that radiation is additionally provided with the tube furnace
Section is used to heat maltha.
3. tar cooling according to claim 1 and distilling apparatus, it is characterised in that dehydrating tower is also connected with light oil cooler
And oil water separator, light oil cooler is interior to be provided with light oil backflash；Light oil backflash one end is connected to dehydrating tower, light oil backflash
Top connects edible vegetable oil medial launder.
4. tar cooling according to claim 1 and distilling apparatus, it is characterised in that fraction overhead portion connects provided with pipeline
To washing oil condensate cooler.
5. tar cooling according to claim 4 and distilling apparatus, it is characterised in that washing oil condensate cooler and mixed triolein
Washing oil backflash is additionally provided between cooler, the return duct with reflux pump is additionally provided between washing oil backflash and cut tower.
6. tar cooling according to claim 1 and distilling apparatus, it is characterised in that fraction overhead portion is additionally provided with a vacuum
Pump.
7. tar cooling according to claim 1 and distilling apparatus, it is characterised in that tar/carbon black oil heat exchanger connection
Carbon black oil pan tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720818520.2U CN207130213U (en) | 2017-07-07 | 2017-07-07 | A kind of tar cooling and distilling apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720818520.2U CN207130213U (en) | 2017-07-07 | 2017-07-07 | A kind of tar cooling and distilling apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207130213U true CN207130213U (en) | 2018-03-23 |
Family
ID=61633921
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720818520.2U Expired - Fee Related CN207130213U (en) | 2017-07-07 | 2017-07-07 | A kind of tar cooling and distilling apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207130213U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109852413A (en) * | 2019-02-21 | 2019-06-07 | 山西竣铭科技有限公司 | A kind of method of coal tar production modified coal tar pitch |
| CN113384912A (en) * | 2021-05-26 | 2021-09-14 | 中冶焦耐(大连)工程技术有限公司 | Negative pressure single-furnace single-tower industrial naphthalene rectification system and process |
-
2017
- 2017-07-07 CN CN201720818520.2U patent/CN207130213U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109852413A (en) * | 2019-02-21 | 2019-06-07 | 山西竣铭科技有限公司 | A kind of method of coal tar production modified coal tar pitch |
| CN113384912A (en) * | 2021-05-26 | 2021-09-14 | 中冶焦耐(大连)工程技术有限公司 | Negative pressure single-furnace single-tower industrial naphthalene rectification system and process |
| CN113384912B (en) * | 2021-05-26 | 2024-05-14 | 中冶焦耐(大连)工程技术有限公司 | Negative pressure single-furnace single-tower industrial naphthalene rectification system and process |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20181022 Address after: 056503 North Village of Chen Zhuang village, Cixian village, Handan, Hebei (Cixian Coal Chemical Industry Park) Patentee after: Cixian Xinbao Chemical Co., Ltd. Address before: 056500 North Village of Chen Zhuang village, Cixian village, Handan, Hebei (Cixian Coal Chemical Industry Park) Patentee before: Handan Xinbao coalification energy science and technology development limited company |
|
| TR01 | Transfer of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20180323 Termination date: 20190707 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |