CN102408298A - Method of distilling crude benzene by decompression method and device thereof - Google Patents
Method of distilling crude benzene by decompression method and device thereof Download PDFInfo
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- CN102408298A CN102408298A CN2011102798811A CN201110279881A CN102408298A CN 102408298 A CN102408298 A CN 102408298A CN 2011102798811 A CN2011102798811 A CN 2011102798811A CN 201110279881 A CN201110279881 A CN 201110279881A CN 102408298 A CN102408298 A CN 102408298A
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Abstract
The invention relates to a method of distilling crude benzene by decompression method and a device thereof. Rich oil is preheated to 165-175 degrees centigrade after being subjected to heat exchange through an oil gas heat exchanger and a rich and poor oil heat exchanger; the rich oil enters in a crude benzene tower for crude benzene distillation; the crude benzene product is extracted from the tower top, and one part of the poor oil at the tower bottom is returned to the crude benzene tower as the distilling heat source after being heated by a tubular furnace while the other part of the poor oil is returned to a benzene washing tower after being subjected to heat exchanging and cooling; and the crude benzene steam escaped from the tower top enters in a crude benzene reflux groove after being cooled by the oil gas heat exchanger and a crude benzene condensing cooler, one part of the crude benzene steam is conveyed to the tower top as the back flow by a crude benzene reflux pump while the other part of the crude benzene steam enters in a crude benzene storage groove, and the crude benzene products are pumped to an oil depot. The lower part of the oil gas heat exchanger is connected with a crude benzene middle groove and is connected to a vacuum pump; the oil gas heat exchanger is connected with the crude benzene tower through the poor and rich oil heat exchanger; the bottom of the crude benzene tower is connected with the tubular furnace through a crude benzene tower circulation pump; and the tubular furnace is connected with a regeneration tower. The invention has the advantages of energy saving, emission reduction, environment protection, synergistic effect, low investment, small floor area, device reliability and flexibility and the like.
Description
Technical field
The present invention relates to the technology of coke oven gas purification system recoveries crude benzol, belong to the coking engineering projects technology, be specifically related to a kind of improved decompression method crude benzol distillating method and device thereof.
Background technology
At present, the crude benzol distil process of domestic majority mainly adopts the method for water at atmospheric pressure steam stripping, and its basic technology is to utilize single tower to produce crude benzol or light benzene under the normal pressure, this technical maturity, stable, but in still-process, can produce a large amount of waste water.
More domestic technician have done some to existing technology and have improved the method and apparatus (patent No. CN101544913A) that the Chinese patent document discloses a kind of negative pressure benzene removal on September 30th, 2009.Its technology forms negative pressure for using vacuum pump to debenzolizing tower and revivifier, at the bottom of the debenzolizing tower tower with regenerator column at the bottom of the cancellation steam stripping, adopt two tubular ovens to carry out at the bottom of the tower circulation respectively and heat thermal source is provided.The debenzolizing tower rectifying section adopts filler to separate light benzene and heavy benzol, and this technology has reduced the temperature of debenzolizing tower cat head, has cancelled steam heating, in energy-conserving and environment-protective, has made certain contribution.But this technology has increased vacuum pump, a regeneration tubular oven and many recycle pumps, and it is more that investment and floor space are increased; The power consumption increase is very big; Make tube furnace heating rich oil because of system adopts negative-pressure operation in addition, the possibility of vaporization increases considerably in the stove; Tower body is high, and the column plate number of plies is many.
In view of this, seek a kind of method crude benzol distillating method and device thereof of reducing pressure and become pursuing one's goal of these those skilled in the art.
Summary of the invention
Task of the present invention provides a kind of decompression method crude benzol distillating method and device thereof; It has overcome above-mentioned existing in prior technology shortcoming; Provide a kind of investment low, the adaptation of product is strong, stable operation is flexible, energy consumption is low, is difficult for the tube oven method decompression crude benzol distil process and the device thereof of coking.
Technical solution of the present invention is following:
A kind of decompression method crude benzol distillating method may further comprise the steps:
(1) is preheated to 165 ℃ to 175 ℃ after rich oil process oil gas interchanger and the poor oil-rich heat exchanger heat exchange;
(2) rich oil entering crude benzol tower carries out the crude benzol distillation;
(3) cat head extraction crude benzol product, the oil-poor part at the bottom of the tower is returned the crude benzol tower after the tube furnace heating, and as the distillation thermal source, oil-poor after the heat exchange cooling, the getting back to of another part washed the benzene tower;
The crude benzol steam that cat head is overflowed gets into the crude benzol backflash after oily vapour interchanger, the cooling of crude benzol condensate cooler, part crude benzol steam is delivered to cat head as backflow with the crude benzol reflux pump, and all the other crude benzol steam get into the crude benzol storage tank, deliver to oil depot with the crude benzol product pump again.
Oil-poorly in the said step (3) extract out through the debenzolizing tower recycle pump, after tube furnace is heated to 225 ℃ to 239 ℃, send debenzolizing tower back at the bottom of.
Said crude benzol column overhead pressure is 15 kPa, and to 50kPa, tower bottom pressure is 25 kPa to 65kPa.
Said crude benzol column overhead temperature is 65 ℃ to 75 ℃, and column bottom temperature is 200 ℃ to 250 ℃.
A kind of decompression method crude benzol water distilling apparatus comprises tube furnace, regenerator column recycle pump, regenerator column, crude benzol tower recycle pump, crude benzol tower, hot oil-poor pump, poor oil-rich heat exchanger, oily vapour interchanger, vacuum pump and crude benzol medial launder;
The bottom of said oily vapour interchanger connects the crude benzol medial launder, and the crude benzol medial launder is connected to vacuum pump;
Said oily vapour interchanger is through the middle part of poor oil-rich heat exchanger connection crude benzol tower, and the top of crude benzol tower connects oily vapour interchanger, and the bottom of crude benzol tower connects poor oil-rich heat exchanger through hot oil-poor pump;
The bottom of said crude benzol tower connects tube furnace through crude benzol tower recycle pump, and tube furnace connects the middle part of regenerator column and crude benzol tower respectively, and regenerator column connects tube furnace through the regenerator column recycle pump, and the top of regenerator column connects the middle part of crude benzol tower.
The number of plies of said crude benzol tower is 34 to 38.
A kind of innovative point that reduces pressure method crude benzol distillating method and device thereof of the present invention is; Wash rich oil that benzene workshop section sees off and be preheated to 165 ℃ to 175 ℃ after through oil gas interchanger and poor oil-rich heat exchanger heat exchange; Directly get into the crude benzol tower without the tubular oven heating and carry out the crude benzol distillation, cat head extraction crude benzol product, side line is adopted naphtalene oil; Oil-poor part at the bottom of the tower is returned the crude benzol tower after the tube furnace heating, as the distillation thermal source; Oil-poor after the heat exchange cooling, the getting back to of another part washed the benzene tower, and wherein: crude benzol column overhead pressure is 15 kPa to 50kPa, and tower bottom pressure is 25 kPa to 65kPa; Tower top temperature is 65 ℃ to 75 ℃, and column bottom temperature is 200 ℃ to 250 ℃.
Preferably, in the decompression crude benzol distil process of the present invention, the rich oil charging is heated without tube furnace, directly gets into the crude benzol tower, and it is little to have a resistance, and throw of pump is low, and is energy-conservation; Have also that vaporization rate is low, corrodibility is little and tube furnace is difficult for advantages such as coking, stable operation, and tradition or other technology power consumption are high and perishable.
Preferably, in the decompression crude benzol distil process of the present invention, take off benzene and regeneration, and adopt biradial chamber independent regulation structure only with a tube furnace, the distinctive tube furnace heat regulation of tool mode, but make all free adjustment temperature of every road heating medium.Whether in addition, regeneration system rapidly can be according to different coke-oven plants practical situation, can select decision to put into operation, even and regeneration system rapidly does not move, the RS Regenerator Section of tube furnace is heating cycle washing oil in addition still, makes tube furnace obtain utilization to greatest extent.
Preferably, in the decompression crude benzol distil process of the present invention, distinctive tray structure pattern, efficient anti-stifled, be fit to the coking dielectric property; Turndown ratio is fit to the coke oven capacity variation; Product is the high-quality crude benzol, can satisfy the specification of quality of benzene hydrogenation device to the raw material crude benzol.
Preferably, in the decompression crude benzol distil process of the present invention, the column plate number of plies is few, general 34 to 38, lacks nearly 20 than the light benzene tower; Side line can be adopted naphtalene oil but not adopt heavy benzol; Column bottom temperature is low, can prevent that circulating washing oil is rotten because of heat.
Preferably, in the decompression crude benzol distil process of the present invention, vacuum system with non-water class medium as the pendular ring medium, non-wastewater discharge, environment protecting is good.
Preferably, in the decompression crude benzol distil process of the present invention, near tower opening for feed place, remote valve is set, to prevent the vaporizing corrosion boiler tube in the heating medium stove at stove exit.
In the above-mentioned modified version decompression crude benzol distil process, adopt the oily water separation of distinctive simple and practical crude benzol backflash; Oil vapour interchanger selects not stop up corrosion resistant Taper Pipe interchanger.
The present invention makes it compared with prior art owing to adopted above technical scheme, the invention has the advantages that energy-conservation, reduction of discharging, environmental protection, synergy, all respects such as investment is low, floor space is little, device reliability and handiness.Wherein: aspect energy-conservation: save coal gas more than 20%; Reduce discharging: do not have newly-increased spent process water; Environmental protection: subnormal ambient has the benzene class material of great bodily injury to be difficult for revealing to human body; Synergy: the yield of crude benzol has improved 0.05 to 0.15%; Investment is low little with floor space: because of reducing by a stove, investment and floor space are all reduced to some extent; Device reliability: the rich oil charging is heated without tube furnace, have do not vaporize, advantages such as noncoking, low corrosion; Whether the device handiness: regeneration system rapidly can be according to different coke-oven plants practical situation, can select decision to put into operation, even and regeneration system rapidly does not move, the RS Regenerator Section of tube furnace is heating cycle washing oil in addition still, makes tube furnace obtain utilization to greatest extent.
Description of drawings
Fig. 1 is the structural representation of a kind of method crude benzol water distilling apparatus that reduces pressure of the present invention.
Reference numeral:
1 is tube furnace, and 2 is the regenerator column recycle pump, and 3 is regenerator column, and 4 is crude benzol tower recycle pump, and 5 is naphtalene oil, and 6 is the crude benzol tower, and 7 is hot oil-poor pump, and 8 is poor oil-rich heat exchanger, and 9 is oil-poor, and 10 is rich oil, and 11 is oily vapour interchanger, and 12 is vacuum pump, and 13 is the crude benzol medial launder.
Embodiment
Below in conjunction with accompanying drawing and embodiment the present invention is elaborated.
The invention provides a kind of decompression method crude benzol distillating method, may further comprise the steps:
(1) is preheated to 165 ℃ to 175 ℃ after rich oil process oil gas interchanger and the poor oil-rich heat exchanger heat exchange.
(2) rich oil entering crude benzol tower carries out the crude benzol distillation.
(3) cat head extraction crude benzol product, the oil-poor part at the bottom of the tower is returned the crude benzol tower after the tube furnace heating, and as the distillation thermal source, oil-poor after the heat exchange cooling, the getting back to of another part washed the benzene tower.
In the said step (3); The crude benzol steam that cat head is overflowed gets into the crude benzol backflash after oily vapour interchanger, the cooling of crude benzol condensate cooler, part crude benzol steam is delivered to cat head as backflow with the crude benzol reflux pump; All the other crude benzol steam get into the crude benzol storage tank, deliver to oil depot with the crude benzol product pump again.
In the said step (3), oil-poorly extract out through the debenzolizing tower recycle pump, after tube furnace is heated to 225 ℃ to 239 ℃, send debenzolizing tower back at the bottom of.
Crude benzol column overhead pressure is 15 kPa, and to 50kPa, tower bottom pressure is 25 kPa to 65kPa.
Crude benzol column overhead temperature is 65 ℃ to 75 ℃, and column bottom temperature is 200 ℃ to 250 ℃.
Referring to Fig. 1; The invention provides a kind of decompression method crude benzol water distilling apparatus, it mainly is made up of tube furnace 1, regenerator column recycle pump 2, regenerator column 3, crude benzol tower recycle pump 4, crude benzol tower 6, hot oil-poor pump 7, poor oil-rich heat exchanger 8, oily vapour interchanger 11, vacuum pump 12 and crude benzol medial launder 13.
The bottom of oil vapour interchanger 11 connects crude benzol medial launder 13, and crude benzol medial launder 13 is connected to vacuum pump 12.Oil vapour interchanger 11 is through the middle part of poor oil-rich heat exchanger 8 connection crude benzol towers 6, and the top of crude benzol tower 6 connects oily vapour interchanger 11, and the bottom of crude benzol tower 6 connects poor oil-rich heat exchangers 8 through hot oil-poor pump 7.
The bottom of crude benzol tower 6 connects tube furnace 1 through crude benzol tower recycle pump 4, and tube furnace 1 connects the middle part of regenerator column 3 and crude benzol tower 6 respectively, and regenerator column 3 connects tube furnace 1 through regenerator column recycle pump 2, and the top of regenerator column 3 connects the middle part of crude benzol tower 6.The number of plies of crude benzol tower 6 is 34 to 38.
The actual use-pattern of decompression method crude benzol distillating method of the present invention and device thereof is following:
Certain coke-oven plant coking engineering projects gas cleaning system crude benzol distillation workshop section has adopted above-mentioned decompression crude benzol distil process, and concise and to the point technical process is following:
The rich oil of sending here from whole cold wash benzene device warp let-off oil vapour interchanger, poor oil-rich heat exchanger (without the tube furnace heating) heat exchange to 165 successively ℃ gets into debenzolizing tower after 175 ℃.At the bottom of the debenzolizing tower road heat is oil-poor extracts out through the debenzolizing tower recycle pump, after tube furnace is heated to 225 ℃ to 239 ℃, send debenzolizing tower back at the bottom of, as debenzolizing tower distillatory thermal source.The crude benzol steam that cat head is overflowed gets into the crude benzol backflash after oily vapour interchanger, the cooling of crude benzol condensate cooler, part is delivered to cat head as backflow with the crude benzol reflux pump, and all the other get into the crude benzol storage tank, deliver to oil depot with the crude benzol product pump again.
Hot oil-poor with what discharge at the bottom of the hot oil-poor pump extraction debenzolizing tower, after the poor oil-rich heat exchanger heat exchange, get into one section oil-poor water cooler, go into oil-poor groove after the cooling, extract out with cold oil-poor pump then and after two sections oil-poor water coolers are cooled to 27 ℃～29 ℃, remove whole cold wash benzene device.
The noncondensable gas of discharging from crude benzol backflash top is delivered to vacuum pump after the cooling of noncondensable gas water cooler; In the cleaned coal feed channel of after vacuum pump is extracted out, delivering coal; Regulate the working pressure at debenzolizing tower top at this with the vacuum suction amount of vacuum pump, it is operated under suitable condition of negative pressure.
Draw the naphtalene oil fraction at the debenzolizing tower side line, to reduce the oil-poor naphthalene that contains.
From tube furnace outlet circulating washing oil, draw 1%～2% hot washing oil, send into regeneration in the regenerator column.Hot washing oil at the bottom of the regenerator column is extracted out through the regenerator column recycle pump, after tube furnace is heated to 240 ℃ to 265 ℃, send regenerator column back at the bottom of, as regenerator column distillatory thermal source.Regeneration overhead gas gets into debenzolizing tower, draws one road Residual oil from the regenerator column circulating-pump outlet in addition and delivers in the naphtalene oil groove, again with pumping oil depot or the cold workshop section of drum.
Multiple advantages such as in sum, decompression method crude benzol distillating method of the present invention and device thereof have energy-conservation, reduction of discharging, environmental protection, synergy, investment is low, floor space is little, device reliability and handiness.
Certainly; Those skilled in the art in the present technique field will be appreciated that; The foregoing description only is to be used for explaining the present invention; And be not with opposing qualification of the present invention, as long as in connotation scope of the present invention, all will drop in the scope of claim of the present invention the variation of the foregoing description, modification etc.
Claims (6)
1. a decompression method crude benzol distillating method is characterized in that, may further comprise the steps:
(1) is preheated to 165 ℃ to 175 ℃ after rich oil process oil gas interchanger and the poor oil-rich heat exchanger heat exchange;
(2) rich oil entering crude benzol tower carries out the crude benzol distillation;
(3) cat head extraction crude benzol product, the oil-poor part at the bottom of the tower is returned the crude benzol tower after the tube furnace heating, and as the distillation thermal source, oil-poor after the heat exchange cooling, the getting back to of another part washed the benzene tower;
The crude benzol steam that cat head is overflowed gets into the crude benzol backflash after oily vapour interchanger, the cooling of crude benzol condensate cooler, part crude benzol steam is delivered to cat head as backflow with the crude benzol reflux pump, and all the other crude benzol steam get into the crude benzol storage tank, deliver to oil depot with the crude benzol product pump again.
2. decompression method crude benzol distillating method as claimed in claim 1 is characterized in that: oil-poorly in the said step (3) extract out through the debenzolizing tower recycle pump, after tube furnace is heated to 225 ℃ to 239 ℃, send debenzolizing tower back at the bottom of.
3. decompression method crude benzol distillating method as claimed in claim 1 is characterized in that: said crude benzol column overhead pressure is 15 kPa, and to 50kPa, tower bottom pressure is 25 kPa to 65kPa.
4. decompression method crude benzol distillating method as claimed in claim 1 is characterized in that: said crude benzol column overhead temperature is 65 ℃ to 75 ℃, and column bottom temperature is 200 ℃ to 250 ℃.
5. a decompression method crude benzol water distilling apparatus is characterized in that: comprise tube furnace, regenerator column recycle pump, regenerator column, crude benzol tower recycle pump, crude benzol tower, hot oil-poor pump, poor oil-rich heat exchanger, oily vapour interchanger, vacuum pump and crude benzol medial launder;
The bottom of said oily vapour interchanger connects the crude benzol medial launder, and the crude benzol medial launder is connected to vacuum pump;
Said oily vapour interchanger is through the middle part of poor oil-rich heat exchanger connection crude benzol tower, and the top of crude benzol tower connects oily vapour interchanger, and the bottom of crude benzol tower connects poor oil-rich heat exchanger through hot oil-poor pump;
The bottom of said crude benzol tower connects tube furnace through crude benzol tower recycle pump, and tube furnace connects the middle part of regenerator column and crude benzol tower respectively, and regenerator column connects tube furnace through the regenerator column recycle pump, and the top of regenerator column connects the middle part of crude benzol tower.
6. decompression method crude benzol water distilling apparatus as claimed in claim 5 is characterized in that: the number of plies of said crude benzol tower is 34 to 38.
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| CN201110279881.1A CN102408298B (en) | 2011-09-21 | 2011-09-21 | Method of distilling crude benzene by decompression method and device thereof |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102796571A (en) * | 2012-07-25 | 2012-11-28 | 济钢集团国际工程技术有限公司 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
| CN102827646A (en) * | 2012-09-07 | 2012-12-19 | 云南大为制焦有限公司 | Coke oven gas debenzolization system |
| CN103673647A (en) * | 2013-12-03 | 2014-03-26 | 天津华能北方热力设备有限公司 | Method and equipment for heating benzene-washing rich oil with coke oven flue exhaust gas waste heat |
| CN103801099A (en) * | 2014-02-26 | 2014-05-21 | 北京首钢国际工程技术有限公司 | Negative-pressure distillation process system for integrated debenzolization and regeneration tower |
| CN104312638A (en) * | 2014-10-30 | 2015-01-28 | 济南冶金化工设备有限公司 | Thermal coupling negative pressure debenzolizing and regenerating integrated device |
| CN104327864A (en) * | 2014-11-15 | 2015-02-04 | 马钢(集团)控股有限公司 | Cooling system and cooling method of recycle gas in inlet of coke dry quenching furnace |
| CN104403704A (en) * | 2014-11-21 | 2015-03-11 | 中冶焦耐工程技术有限公司 | Negative-pressure crude benzene distillation process and equipment heating washing oil by steam |
| CN104910972A (en) * | 2015-06-26 | 2015-09-16 | 山东钢铁股份有限公司 | Rich oil debenzolization system for processing coke oven gas |
| CN104927929A (en) * | 2015-06-29 | 2015-09-23 | 济南冶金化工设备有限公司 | Crude benzene distilling and washing oil regenerating heating system and method |
| CN104961620A (en) * | 2015-06-03 | 2015-10-07 | 马钢(集团)控股有限公司 | Method for treating benzene hydrogenated polymer |
| CN105154144A (en) * | 2015-08-31 | 2015-12-16 | 山东铁雄新沙能源有限公司 | Negative-pressure debenzylation device and negative-pressure debenzolization method |
| CN107628923A (en) * | 2017-09-29 | 2018-01-26 | 王书虎 | A kind of negative pressure benzene removal system and method for rich oil half |
| CN114292659A (en) * | 2022-01-25 | 2022-04-08 | 枣庄杰富意振兴化工有限公司 | Coal tar deep processing method |
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Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102796571A (en) * | 2012-07-25 | 2012-11-28 | 济钢集团国际工程技术有限公司 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
| CN102796571B (en) * | 2012-07-25 | 2014-04-30 | 济钢集团国际工程技术有限公司 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
| CN102827646A (en) * | 2012-09-07 | 2012-12-19 | 云南大为制焦有限公司 | Coke oven gas debenzolization system |
| CN102827646B (en) * | 2012-09-07 | 2014-03-26 | 云南大为制焦有限公司 | Coke oven gas debenzolization system |
| CN103673647A (en) * | 2013-12-03 | 2014-03-26 | 天津华能北方热力设备有限公司 | Method and equipment for heating benzene-washing rich oil with coke oven flue exhaust gas waste heat |
| CN103801099A (en) * | 2014-02-26 | 2014-05-21 | 北京首钢国际工程技术有限公司 | Negative-pressure distillation process system for integrated debenzolization and regeneration tower |
| CN104312638A (en) * | 2014-10-30 | 2015-01-28 | 济南冶金化工设备有限公司 | Thermal coupling negative pressure debenzolizing and regenerating integrated device |
| CN104327864A (en) * | 2014-11-15 | 2015-02-04 | 马钢(集团)控股有限公司 | Cooling system and cooling method of recycle gas in inlet of coke dry quenching furnace |
| CN104403704A (en) * | 2014-11-21 | 2015-03-11 | 中冶焦耐工程技术有限公司 | Negative-pressure crude benzene distillation process and equipment heating washing oil by steam |
| CN104961620A (en) * | 2015-06-03 | 2015-10-07 | 马钢(集团)控股有限公司 | Method for treating benzene hydrogenated polymer |
| CN104910972A (en) * | 2015-06-26 | 2015-09-16 | 山东钢铁股份有限公司 | Rich oil debenzolization system for processing coke oven gas |
| CN104927929A (en) * | 2015-06-29 | 2015-09-23 | 济南冶金化工设备有限公司 | Crude benzene distilling and washing oil regenerating heating system and method |
| CN105154144A (en) * | 2015-08-31 | 2015-12-16 | 山东铁雄新沙能源有限公司 | Negative-pressure debenzylation device and negative-pressure debenzolization method |
| CN107628923A (en) * | 2017-09-29 | 2018-01-26 | 王书虎 | A kind of negative pressure benzene removal system and method for rich oil half |
| CN114292659A (en) * | 2022-01-25 | 2022-04-08 | 枣庄杰富意振兴化工有限公司 | Coal tar deep processing method |
| CN114292659B (en) * | 2022-01-25 | 2023-09-01 | 枣庄杰富意振兴化工有限公司 | Deep processing method of coal tar |
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