CN104974776A - Tar distillation device - Google Patents
Tar distillation device Download PDFInfo
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- CN104974776A CN104974776A CN201510295689.XA CN201510295689A CN104974776A CN 104974776 A CN104974776 A CN 104974776A CN 201510295689 A CN201510295689 A CN 201510295689A CN 104974776 A CN104974776 A CN 104974776A
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- output terminal
- tower
- tar
- heating zone
- distillation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/04—Working-up tar by distillation
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a tar distillation device comprising a dehydration tower bottom extraction pump, a first tubular heating furnace, a first distillation tower, a second tubular heating furnace, and a first distillation tower bottom extraction pump. The dehydration tower bottom extraction pump is used for pumping anhydrous tar from a dehydration tower. The first tubular heating furnace comprises a first heating section and a second heating section, wherein an input end of the first heating section is connected with the dehydration tower bottom extraction pump. The first distillation tower comprises a first input end, a second input end, a first output end and a second output end, wherein the first input end is connected with the output end of the first heating section. The input end of the second tubular heating furnace is connected with the first output end through a first distillation bottom circulation pump. An output end of the second tubular heating furnace is connected with the second input end. The input end of the first distillation tower bottom extraction pump is connected with the second output end. The output end of the first distillation tower bottom extraction pump is connected with the input end of the second heating section. With the above technical scheme, a technical problem of tubular heating furnace tube coking in prior arts is solved; furnace tube coking is avoided; and production period is prolonged.
Description
Technical field
The present invention relates to extensive tar production technical field, particularly a kind of tar distillation device.
Background technology
Tar distillation adopts circulating-heating technique at the bottom of air distillation, underpressure distillation, multi-tower type, tower.Please refer to Fig. 1, in the technique of the distillation of prior art, extract delivery side of pump at the bottom of dehydration tower tower out and be connected with the circulation tube of 1# distillation tower, and enter the boiler tube of the second tubular oven by same pipeline.Extractor pump is to the circulation tube of the first distillation tower, the second tubular oven charging at the bottom of dehydration tower tower for tar, and the circulation tube of the first distillation tower is to the boiler tube charging of the second tubular oven.
But, the caliber of the circulation tube of the first distillation tower is larger to the caliber of the feed-pipe of the first input of column than dehydration tower extractor pump, dehydration tower extractor pump lift is 110m, feed-pipe pressure can reach nearly 10 kilograms, circulation tube pressure is less than 4 kilograms, the fluid of such high pressure low temperature enters the situation that just there will be flash distillation in the environment of low-voltage high-temperature, flash distillation causes producing a large amount of bubble in circulation tube, and enter the boiler tube of the second tubular oven, because rate of flow of fluid reaches nearly 2.1m/s, under the effect of spiral centrifugal power, bubble boiler tube centripetal oblique above flowing, cause boiler tube local temperature too high, cause the tube coking of the second tubular oven, the production cycle is caused to shorten.
Visible, there is the technical problem of tubular oven tube coking in the coal-tar middle oil water distilling apparatus of prior art.
Summary of the invention
The embodiment of the present invention provides a kind of tar distillation device, for solving the technical problem of the tubular oven tube coking that the coal-tar middle oil water distilling apparatus of prior art exists, avoiding tube coking, extending manufacture cycle.
The embodiment of the present application provides a kind of tar distillation device, and described water distilling apparatus comprises:
Extractor pump at the bottom of dehydration tower, for extracting anhydrous tar out from dehydration tower;
First tubular oven, comprises the first heating zone and the second heating zone, and the input terminus of described first heating zone is connected with extractor pump at the bottom of described dehydration tower;
First distillation tower, comprises first input end, the second input terminus, the first output terminal and the second output terminal, and described first input end is connected with the output terminal of described first heating zone;
Second tubular oven, the input terminus of described second tubular oven is connected with described first output terminal by the first base product recycle pump, and the output terminal of described second tubular oven is connected with described second input terminus;
First base product extractor pump, the input terminus of described first base product extractor pump is connected with described second output terminal, and described first base product is extracted delivery side of pump out and is connected with the input terminus of described second heating zone.
Optionally, described first heating zone is convection zone, and described second heating zone is radiation section.
Optionally, described first distillation tower also comprises:
The first layer traverse baffle, is connected with described first input end, and the charging of described first input end enters described first distillation tower by described the first layer traverse baffle.
Optionally, described water distilling apparatus also comprises:
Second column, comprises the 3rd input terminus, the 3rd output terminal and the 4th output terminal;
Wherein, described 3rd input terminus is connected with the output terminal of described second heating zone, and described 3rd output terminal is connected with the input terminus of described second heating zone by recycle pump at the bottom of second column, and described 4th output terminal is for extracting pitch out.
Optionally, described water distilling apparatus also comprises:
Dehydration tower, is connected with extractor pump at the bottom of described dehydration tower;
Predehydration, is connected with tar preheater with dehydration tower, for dewatering to the raw tar after described tar preheater heating and be separated light oil process, and the tar after process is inputted described dehydration tower.
Above-mentioned one or more technical scheme in the embodiment of the present application, at least has following technique effect:
The embodiment of the present application provides a kind of new tar distillation device, wherein, extractor pump at the bottom of dehydration tower is connected with the output terminal of the first heating zone of the first tubular oven, the output terminal of the first heating zone is connected with the first input end of the first distillation tower, first output terminal and second input terminus and second of the first distillation tower process furnace of running affairs is connected, and the second output terminal of the first distillation tower is connected with the first base product extractor pump.By being connected extracting delivery side of pump at the bottom of dehydration tower out with the first tubular oven, the feed-pipe of extractor pump at the bottom of dehydration tower is separated with the circulation tube of the first base product recycle pump, and then avoid a large amount of bubble of generation in circulation tube to cause the tube coking of the first tubular oven, solve the technical problem of the tubular oven tube coking that the coal-tar middle oil water distilling apparatus of prior art exists, avoid tube coking, extend the production cycle.
Accompanying drawing explanation
Fig. 1 is charging and the distillation schematic diagram of tar distillation device of the prior art;
The schematic diagram of a kind of tar distillation device that Fig. 2 provides for the embodiment of the present application;
The schematic diagram of the second column that Fig. 3 provides for the embodiment of the present application, dehydration tower and predehydration.
Embodiment
In the technical scheme that the embodiment of the present application provides, by the circulation tube of the feed-pipe of extractor pump at the bottom of dehydration tower with the first base product recycle pump is separated, to avoid producing in circulation tube the tube coking that a large amount of bubble causes tubular oven, thus solve the technical problem of the tubular oven tube coking that the coal-tar middle oil water distilling apparatus of prior art exists, avoid tube coking, extend manufacture cycle.
Below in conjunction with accompanying drawing, the main of the embodiment of the present application technical scheme is realized principle, embodiment and be explained in detail the beneficial effect that should be able to reach.
Embodiment
Please refer to Fig. 2, the embodiment of the present application provides a kind of tar distillation device, and described water distilling apparatus comprises:
Extractor pump 201 at the bottom of dehydration tower, for extracting anhydrous tar out from dehydration tower;
First tubular oven 202, comprises the first heating zone and the second heating zone, and the input terminus of described first heating zone is connected with extractor pump 201 at the bottom of described dehydration tower;
First distillation tower 203, comprises first input end, the second input terminus, the first output terminal and the second output terminal, and described first input end is connected with the output terminal of described first heating zone;
Second tubular oven 204, the input terminus of described second tubular oven 204 is connected with described first output terminal by the first base product recycle pump 205, and the output terminal of described second tubular oven 204 is connected with described second input terminus;
First base product extractor pump 206, the input terminus of described first base product extractor pump 206 is connected with described second output terminal, and the output terminal of described first base product extractor pump 206 is connected with the input terminus of described second heating zone.
Please refer to Fig. 3, in specific implementation process, the tar distillation device that the embodiment of the present application provides also comprises: dehydration tower 210 and predehydration 211.Wherein, dehydration tower 210 is connected with extractor pump at the bottom of dehydration tower 201; Predehydration 211 is connected with tar preheater 212 with dehydration tower 210, carries out dewatering and being separated light oil process for the raw tar after oil preheater 212 of focusing heats, and by the tar input dehydration tower 210 after process.Dehydration tower 210 is also connected with recycle pump at the bottom of dehydration tower 214, at the bottom of dehydration tower, recycle pump 214 is connected with dehydration tower reboiler 213, dehydration tower reboiler 213 is also connected with dehydration tower 210, makes recycle pump 214 at the bottom of dehydration tower 210, dehydration tower and dehydration tower reboiler 213 form a circulation.Tar bottom dehydration tower 210 is retracted in dehydration tower reboiler 213 and heats by recycle pump 214 at the bottom of dehydration tower, tar after heating re-enters dehydration tower 210 to carry out dewatering and being separated light oil process again, to reach the object of tar being carried out to fully dehydration, obtain anhydrous tar, make extractor pump 201 at the bottom of dehydration tower can extract anhydrous tar out from dehydration tower 210.
At the bottom of dehydration tower, the output terminal of extractor pump 201 is feed-pipe, is connected with the first tubular oven 202.Concrete, the first tubular oven 202 comprises the first heating zone and the second heating zone, and at the bottom of dehydration tower, the output terminal of extractor pump 201 is connected with the input terminus of the first heating zone.Wherein, first heating zone is convection zone, second heating zone is radiation section, convection zone and radiation section are separated from each other, when the convection zone avoiding the anhydrous tar of extractor pump 201 extraction at the bottom of dehydration tower to input the first tubular oven 202 heats, affect the heating operation of radiation section in the first tubular oven 202.
The output terminal of the first heating zone of the first tubular oven 202 is connected with the input terminus of the first distillation tower 203 and feed end, makes the anhydrous tar heated through the first heating zone to the first distillation tower 203 charging.Multilayer traverse baffle is comprised, for successively distilling the effect improving distillation in first distillation tower 203.In first distillation tower 203, the first layer traverse baffle 203a is the superiors' traverse baffle, so the first input end of the first distillation tower 203 is connected with the first layer traverse baffle 203a by the embodiment of the present application, make the charging of first input end enter the first distillation tower 203 by the first layer traverse baffle 203a, thus can successively distill.
In order to improve the distilling effect of the first distillation tower 203 further, the first distillation tower 203 is also provided with the second input terminus and the first output terminal.First output terminal is connected with the input terminus of the first base product recycle pump 205, the output terminal of the first base product recycle pump 205 and circulation tube are connected with the input terminus of the second tubular oven 204, and the output terminal of the second tubular oven 204 is connected with the second input terminus of the first distillation tower 203.For this reason, Matter Transfer bottom first distillation tower 203 can be extracted out by the first base product recycle pump 205 by the embodiment of the present application, and be input to the second tubular oven 204 and heat, inputted the first distillation tower 203 by the logistics recirculation after heating and carry out circulation distillation.
First distillation tower 203 is also provided with the second output terminal, is connected with the input terminus of the first base product extractor pump 206, and the output terminal of the first base product extractor pump 206 is connected with the input terminus of the second heating zone.First base product extractor pump 206 extracts heavy mixing oil out from first distillation tower 203 end, and inputs the first tubular oven 202 and heat, the heavy mixing oil input second column 207 after the first tubular oven 202 heats.
Second column 207, comprises the 3rd input terminus, the 3rd output terminal and the 4th output terminal.Wherein, the 3rd input terminus of second column 207 is connected with the output terminal of the second heating zone of the first tubular oven 202; 3rd output terminal of second column 207 is connected with the input terminus of the second heating zone of the first tubular oven 202 by recycle pump 208 at the bottom of second column; 4th output terminal of second column 207 is connected with extractor pump at the bottom of second column 209, extracts pitch by extractor pump at the bottom of second column 209 out from the bottom of second column 207.
Please refer to Fig. 3, below the distil process of the water distilling apparatus that the embodiment of the present application provides be described in detail:
One, dewater
Raw tar is through washing oil interchanger 217, naphtalene oil interchanger 218, one carbolineum interchanger 219 respectively with product washing oil, naphtalene oil, after one carbolineum heat exchange, through tar preheater 212, (employing thermal oil is heating medium again, thermal oil is by product asphalt heating) be heated to about 120 DEG C, enter after predehydration 211 deviates from part water and part light oil and enter dehydration tower 210, dehydration tower 210 is mainly used to fully dehydration and extraction light oil at present, tower bed coke oil is delivered to by dehydration tower reboiler 213 circulating-heating of heat-conducting oil heating to about 190 DEG C by dehydration tower recycle pump 214 by dehydration tower 210 end, double tower dehydration is adopted to ensure that the stability of whole Distallation systm.
Two, distill
By extractor pump at the bottom of dehydration tower 201 from extraction anhydrous tar at the bottom of tower, after convection zone anhydrous tar being delivered to the first tubular oven 202 is heated to 300 DEG C, from the first layer traverse baffle 203a charging of the first distillation tower 203, first distillation tower 203 extraction carbolic oil successively, naphtalene oil, the tower top of the first distillation tower 203 adopts dephlegmator 215 condensation total reflux, non-condensable gases is by vent condenser laggard death of monks or nuns cigarette groove, extract raw material out by the first distillation tower recycle pump 205 at the bottom of tower and export the second tubular oven 204 to through circulation tube, after about the second tubular oven 204 circulating-heating to 320 DEG C, input back the first distillation tower 203 to circulate distillation, after first distillation tower 203 end extraction heavy mixing oil, be drawn to the radiation section charging of the first tubular oven 202 by the first distillation tower extractor pump 206, after the radiation section heating of the first tubular oven 202, export second column 207 circulation distillation to, pitch bottom second column 207 extracts the radiation section also sending into the first tubular oven 202 out by second column recycle pump 208, circulating-heating exports second column 207 circulation distillation to after about 355 DEG C.
Three, extraction
Second column 207, in the process of distillation, distinguishes extraction washing oil, a carbolineum, anthracene oil, mid-temperature pitch, or extraction washing oil, a carbolineum, viscid bitumen respectively, its medium pitch is extracted out by extractor pump at the bottom of second column 209.The tower top of second column 207 adopts dephlegmator 216 condensation total reflux, and non-condensable gases is by being gone out cigarette groove by vacuum pump suction after vent condenser, and the tower top vacuum cavitations of second column 207 is at-80KPa.
By the one or more technical schemes in the embodiment of the present application, following technique effect can be realized:
The embodiment of the present application provides and is connected by the output terminal of extractor pump at the bottom of dehydration tower with the first heating zone of the first tubular oven, the output terminal of the first heating zone is connected with the first input end of the first distillation tower, first output terminal and second input terminus and second of the first distillation tower process furnace of running affairs is connected, and the second output terminal of the first distillation tower is connected with the first base product extractor pump.By being connected extracting delivery side of pump at the bottom of dehydration tower out with the first tubular oven, the feed-pipe of extractor pump at the bottom of dehydration tower is separated with the circulation tube of the first base product recycle pump, and then avoid a large amount of bubble of generation in circulation tube to cause the tube coking of the first tubular oven, solve the technical problem of the tubular oven tube coking that the coal-tar middle oil water distilling apparatus of prior art exists, avoid tube coking, extend the production cycle.
Although describe the preferred embodiments of the present invention, those skilled in the art once obtain the basic creative concept of cicada, then can make other change and amendment to these embodiments.So claims are intended to be interpreted as comprising preferred embodiment and falling into all changes and the amendment of the scope of the invention.
Obviously, those skilled in the art can carry out various change and modification to the present invention and not depart from the spirit and scope of the present invention.Like this, if these amendments of the present invention and modification belong within the scope of the claims in the present invention and equivalent technologies thereof, then the present invention is also intended to comprise these change and modification.
Claims (5)
1. a tar distillation device, is characterized in that, described water distilling apparatus comprises:
Extractor pump at the bottom of dehydration tower, for extracting anhydrous tar out from dehydration tower;
First tubular oven, comprises the first heating zone and the second heating zone, and the input terminus of described first heating zone is connected with extractor pump at the bottom of described dehydration tower;
First distillation tower, comprises first input end, the second input terminus, the first output terminal and the second output terminal, and described first input end is connected with the output terminal of described first heating zone;
Second tubular oven, the input terminus of described second tubular oven is connected with described first output terminal by the first base product recycle pump, and the output terminal of described second tubular oven is connected with described second input terminus;
First base product extractor pump, the input terminus of described first base product extractor pump is connected with described second output terminal, and described first base product is extracted delivery side of pump out and is connected with the input terminus of described second heating zone.
2. device as claimed in claim 1, it is characterized in that, described first heating zone is convection zone, and described second heating zone is radiation section.
3. device as claimed in claim 1, it is characterized in that, described first distillation tower also comprises:
The first layer traverse baffle, is connected with described first input end, and the charging of described first input end enters described first distillation tower by described the first layer traverse baffle.
4. the device as described in as arbitrary in claims 1 to 3, it is characterized in that, described water distilling apparatus also comprises:
Second column, comprises the 3rd input terminus, the 3rd output terminal and the 4th output terminal;
Wherein, described 3rd input terminus is connected with the output terminal of described second heating zone, and described 3rd output terminal is connected with the input terminus of described second heating zone by recycle pump at the bottom of second column, and described 4th output terminal is for extracting pitch out.
5. the device as described in as arbitrary in claims 1 to 3, it is characterized in that, described water distilling apparatus also comprises:
Dehydration tower, is connected with extractor pump at the bottom of described dehydration tower;
Predehydration, is connected with tar preheater with described dehydration tower, for dewatering to the raw tar after described tar preheater heating and be separated light oil process, and the tar after process is inputted described dehydration tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510295689.XA CN104974776B (en) | 2015-06-02 | 2015-06-02 | A kind of tar distillation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510295689.XA CN104974776B (en) | 2015-06-02 | 2015-06-02 | A kind of tar distillation device |
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| CN104974776A true CN104974776A (en) | 2015-10-14 |
| CN104974776B CN104974776B (en) | 2017-08-29 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106336888A (en) * | 2016-09-18 | 2017-01-18 | 湖南万容科技股份有限公司 | Pyrolytic oil refining system |
| CN106433762A (en) * | 2016-09-09 | 2017-02-22 | 武汉钢铁股份有限公司 | Production method of coal-series fuel oil |
| EP3498805A4 (en) * | 2016-08-08 | 2019-07-24 | Posco | Process for producing modified tar |
| CN110141884A (en) * | 2019-05-27 | 2019-08-20 | 中冶焦耐(大连)工程技术有限公司 | The method and system of tower top regurgitant volume are controlled in tar production, benzene hydrogenation process |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201305573Y (en) * | 2008-12-11 | 2009-09-09 | 中冶焦耐工程技术有限公司 | Two-tower vacuum tar distilling plant |
-
2015
- 2015-06-02 CN CN201510295689.XA patent/CN104974776B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201305573Y (en) * | 2008-12-11 | 2009-09-09 | 中冶焦耐工程技术有限公司 | Two-tower vacuum tar distilling plant |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3498805A4 (en) * | 2016-08-08 | 2019-07-24 | Posco | Process for producing modified tar |
| CN106433762A (en) * | 2016-09-09 | 2017-02-22 | 武汉钢铁股份有限公司 | Production method of coal-series fuel oil |
| CN106336888A (en) * | 2016-09-18 | 2017-01-18 | 湖南万容科技股份有限公司 | Pyrolytic oil refining system |
| CN110141884A (en) * | 2019-05-27 | 2019-08-20 | 中冶焦耐(大连)工程技术有限公司 | The method and system of tower top regurgitant volume are controlled in tar production, benzene hydrogenation process |
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| Publication number | Publication date |
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| CN104974776B (en) | 2017-08-29 |
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