CN102796571B - System for producing light benzene by performing negative pressure debenzolization on rich oil - Google Patents
System for producing light benzene by performing negative pressure debenzolization on rich oil Download PDFInfo
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- CN102796571B CN102796571B CN201210259143.5A CN201210259143A CN102796571B CN 102796571 B CN102796571 B CN 102796571B CN 201210259143 A CN201210259143 A CN 201210259143A CN 102796571 B CN102796571 B CN 102796571B
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Abstract
The invention provides a system for producing light benzene by performing negative pressure debenzolization on rich oil. The system comprises a debenzolization tower, wherein the top of the debenzolization tower is communicated with a light benzene condensation cooler through a light benzene steam pipeline, the light benzene condensation cooler is communicated with a light benzene return tank through a cooling liquid introducing pipe and a pressure balancing pipe, the light benzene return tank is connected with a light benzene return groove through a light benzene discharge pipe, the light benzene return groove is connected with the debenzolization tower through a light benzene return pipe, the light benzene return tank is provided with a non-condensable gas discharge pipe, the non-condensable gas discharge pipe is communicated with a tubular heat exchanger, a negative pressure pipe is arranged on the tubular heat exchanger, and the negative pressure pipe is communicated with a vacuum pump. The system disclosed by the invention can change ordinary pressure operation to negative pressure operation in a rich oil debenzolization distillation process, be conducive to reducing the distillation boiling point of the light benzene at the top of the tower, reduce the load of the light benzene condensation cooler, realize a smaller amount of separated water from the light benzene, eliminate the need of adopting multiple devices to separate the separated water from the light benzene, be conductive to lowering the cost of the devices, avoid great consumption of steam resources and be conductive to reducing environmental pollution.
Description
Technical field
The present invention relates to Coal Chemical Industry rich oil crude benzol Distallation systm, specifically a kind of light benzene extraction system of rich oil negative pressure benzene removal.
Background technology
At present, the whole cold wash benzene of domestic coke-oven plant gas purification workshop section all adopts tar washing oil or oil washing oil to wash the benzene in coal gas, and washing oil absorbs benzene and becomes rich oil, after the de-benzene of rich oil distillation, becomes washing oil again or claims oil-poor.In order to guarantee the recycle of washing oil, must remove the benzene in rich oil, make it to become and can be sent to whole cold wash benzene workshop section and again wash the oil-poor of benzene.In existing all kinds of processing method, the method that all adopts steamed to blow removes the crude benzol in rich oil, and is to carry out under condition of normal pressure.In production process, due to the thermal source that adopts steam as distillation, therefore, can produce a large amount of reluctant crude benzol Separation of Waters, need to design multiple equipment and separate the Separation of Water in crude benzol and crude benzol, equipment cost taken by themselves is higher.Expended a large amount of steam resources simultaneously, also easily caused serious environmental pollution, the recycling economy index of advocating with country also differs greatly.
Summary of the invention
The object of this invention is to provide a kind of light benzene extraction system of rich oil negative pressure benzene removal, it can change rich oil de-benzene distil process into negative-pressure operation by normal pressure, negative pressure is conducive to reduce the boiling point that distillates of tower top light benzene, alleviated the load of light benzene condensate cooler, energy-saving and cost-reducing, vacuum distillation does not need to adopt the thermal source of steam as distillation, it is less that light benzene separates the water yield, moisture only in rich oil, thereby do not need to adopt the Separation of Water in multiple device separates light benzenes, be conducive to the cost of reduction equipment self, avoid a large amount of consumption of steam resource simultaneously, also help the pollution alleviating environment.
The present invention for achieving the above object, be achieved through the following technical solutions: comprise debenzolizing tower, debenzolizing tower top is communicated with light benzene condensate cooler by light benzene steam pipeline, between light benzene condensate cooler and light benzene return tank, by cooling fluid access tube and pressure equalizing pipe, be communicated with, light benzene return tank bottom arranges separated flow outlet, light benzene return tank is connected with light benzene backflash by light benzene vent pipe, light benzene backflash is connected with debenzolizing tower by light benzene return line, on light benzene return line, reflux pump is installed, light benzene return tank top arranges noncondensable gas vent pipe, noncondensable gas vent pipe is communicated with shell and tube heat exchanger, shell and tube heat exchanger bottom is communicated with light benzene return tank by collector tube, liquid collecting pump and electric-control stop valve are installed on collector tube, negative tube is set on shell and tube heat exchanger, negative tube is communicated with vacuum pump, liquid collecting pump, electric-control stop valve is connected with controller by wire respectively with vacuum pump, controller can automatically cut out electric-control stop valve and liquid collecting pump when vacuum pump is worked, when quitting work, automatically opens by vacuum pump electric-control stop valve and liquid collecting pump, light benzene return tank comprises horizontal tank body, horizontal tank base mid-way is communicated with the top of vertical tank body, horizontal tank base is connected with light benzene vent pipe, vertical tank base arranges separated flow outlet, horizontal inner tank wall arranges annular brace muscle, through hole is offered in annular brace muscle bottom.Cooling fluid access tube extends near horizontal tank base in horizontal tank body, and cooling fluid access tube and light benzene vent pipe are separately positioned on vertical tank body both sides, and overflow plate is installed in the horizontal tank body between light benzene vent pipe and vertical tank body.Cooling fluid access tube lower end arranges hydraucone.In the horizontal inner tank wall at light benzene vent pipe place, vortex shield is set.
The invention has the advantages that: it can change rich oil de-benzene distil process into negative-pressure operation by normal pressure, vacuum distillation does not need to adopt the thermal source of steam as distillation, it is less that light benzene separates the water yield, moisture only in rich oil, thereby do not need to adopt the Separation of Water in multiple device separates light benzenes, reduced the cost of equipment self; Avoid a large amount of consumption of steam resource, also helped the pollution alleviating environment; Light benzene extraction efficiency is high, and can reduce debenzolizing tower tower top light benzene steam extraction temperature, is conducive to reduce the load of condensing cooling device, improves condensation efficiency, and then reaches the effect etc. that improves light benzene organic efficiency.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention; Fig. 2 is the structural representation of light benzene return tank of the present invention.
Embodiment
The light benzene extraction system of a kind of rich oil negative pressure benzene removal of the present invention, comprise debenzolizing tower 1, debenzolizing tower 1 top is communicated with light benzene condensate cooler 3 by light benzene steam pipeline 2, between light benzene condensate cooler 3 and light benzene return tank 4, by cooling fluid access tube 5 and pressure equalizing pipe 6, be communicated with, light benzene return tank 4 bottoms arrange separated flow outlet 7, light benzene return tank 4 is connected with light benzene backflash 9 by light benzene vent pipe 8, light benzene backflash 9 is connected with debenzolizing tower 1 by light benzene return line 10, reflux pump 11 is installed on light benzene return line 10, light benzene return tank 4 tops arrange noncondensable gas vent pipe 12, noncondensable gas vent pipe 12 is communicated with shell and tube heat exchanger 13, shell and tube heat exchanger 13 bottoms are communicated with light benzene return tank 4 by collector tube 14, liquid collecting pump 24 and electric-control stop valve 26 are installed on collector tube 14, negative tube 15 is set on shell and tube heat exchanger 13, negative tube 15 is communicated with vacuum pump 16, liquid collecting pump 24, electric-control stop valve 26 is connected with controller 25 by wire respectively with vacuum pump 16, controller 25 can automatically cut out electric-control stop valve 26 and liquid collecting pump 24 when vacuum pump 16 is worked, when quitting work, automatically opens by vacuum pump 16 electric-control stop valve 26 and liquid collecting pump 24, light benzene return tank 4 comprises horizontal tank body 17, horizontal tank body 17 mid-ways, bottom are communicated with the top of vertical tank body 18, horizontal tank body 17 bottoms are connected with light benzene vent pipe 8, vertical tank body 18 bottoms arrange separated flow outlet 7, horizontal tank body 17 inwalls arrange annular brace muscle 21, through hole 23 is offered in annular brace muscle 21 bottoms.Debenzolizing tower 1, light benzene condensate cooler 3, light benzene return tank 4 and shell and tube heat exchanger 13 all keep negative pressure state under the effect of vacuum pump 16, pressure in vacuum pump 16 and shell and tube heat exchanger 13 is about-60 KPa to-70KPa, pressure in light benzene condensate cooler 3 and light benzene return tank 4 is about-55 KPa to-65 KPa, the pressure of debenzolizing tower 1 tower top is about-50 to-60 KPa aforesaid devices in this pressure range time, light benzene extraction is most effective, and tower top temperature can be controlled to 70 ℃ to 80 ℃, and tower top temperature in currently available technology is all between 90 ℃ to 95 ℃, tower top temperature reduces the load that can effectively reduce condensing cooling device, improve condensation efficiency, and then reach the effect that improves light benzene organic efficiency.Owing to constantly there being cooling fluid in cooling fluid access tube 5, pass through, therefore must between light benzene condensate cooler 3 and light benzene return tank 4, pressure equalizing pipe 6 be set, otherwise the pressure between light benzene condensate cooler 3 and light benzene return tank 4 cannot keep identical the moment, if there is difference in the pressure between light benzene condensate cooler 3 and light benzene return tank 4, can cause raising gradually from light benzene condensate cooler 3 to the each device interior pressure of debenzolizing tower 1, cause cannot keeping desirable negative pressure in debenzolizing tower 1, affect light benzene formation efficiency.The light benzene steam that debenzolizing tower 1 tower top is discharged enters light benzene condensate cooler 3 through light benzene steam pipeline 2, in light benzene condensate cooler 3, condensed cooling fluid enters light benzene return tank 4 through cooling fluid access tube 5, after light benzene is separation with water, Separation of Water is discharged from Separation of Water outlet 7, light benzene enters light benzene backflash 9 through light benzene vent pipe 8, in light benzene backflash 9, a part of light benzene is back to debenzolizing tower 1 through light benzene return line 10 under the effect of reflux pump 11, and remaining light benzene is as product extraction; Gas in light benzene return tank 4 sucks shell and tube heat exchanger 13 under suction function, light benzene steam residual in gas can become phlegma in the interior condensation of shell and tube heat exchanger 13, again get back in light benzene return tank 4 and separate, remaining noncondensable gas enters negative pressure gas line through vacuum pump 16, is convenient to collection and treatment.Because shell and tube heat exchanger 13 inside are negative pressure, therefore liquid collecting pump 24 need be installed on collector tube 14, by liquid collecting pump 24 by the phlegma blowback light benzene return tank 4 in shell and tube heat exchanger 13, when preventing that vacuum pump 16 from working by the gas in light benzene return tank 4 from collector tube 14 suction shell and tube heat exchanger 13, cause reduction of heat exchange efficiency, affect condensation effect, electric-control stop valve 26 need be installed on collector tube 14, when vacuum pump 16 is worked, by electric-control stop valve 26, collector tube 14 is sealed, prevent that gas is from collector tube 14 suction shell and tube heat exchanger 13, be conducive to improve light benzene organic efficiency.Because light benzene return tank 4 tank bodies need bear larger negative pressure pressure, as adopt existing light benzene return tank 4 tank bodies to there will be the situation of Inward deflection, the present invention is for addressing this problem, horizontal tank body 17 inwalls at light benzene return tank 4 arrange annular brace muscle 21, for guaranteeing the liquid conducting of annular brace muscle both sides, in annular brace muscle 21 bottoms, offer through hole 23.The present invention can change rich oil de-benzene distil process into negative-pressure operation by normal pressure, alleviated the load of light benzene condensate cooler, energy-saving and cost-reducing, vacuum distillation does not need to adopt the thermal source of steam as distillation, and it is less that light benzene separates the water yield, moisture only in rich oil, thereby do not need to adopt the Separation of Water in multiple device separates light benzenes, reduce the cost of equipment self, avoided a large amount of consumption of steam resource simultaneously, also helped the pollution alleviating environment.
The present invention is in order to strengthen the light benzene separating effect of light benzene withdrawing can 4, can adopt following structure: cooling fluid access tube 5 extends near horizontal tank body 17 bottoms in horizontal tank body 17, cooling fluid access tube 5 is separately positioned on vertical tank body 18 both sides, the interior installation overflow plate 20 of horizontal tank body 17 between light benzene vent pipe 8 and vertical tank body 18 with light benzene vent pipe 8.Flow velocity when cooling fluid access tube 5 outlet can reduce cooling fluid and enters light benzene return tank 4 near horizontal tank body 17 bottoms, reduce the disturbance of cooling fluid to light benzene return tank 4 interior liquid, overflow plate 20 is separated into two portions by horizontal tank body 17, when liquid level rises to overflow plate 20 tops, just flow to a side that is provided with light benzene vent pipe 8, when cooling fluid enters horizontal tank body 17, the liquid of light benzene vent pipe 8 one sides is subject to disturbance hardly.
Flow velocity when the present invention enters light benzene return tank 4 in order further to reduce cooling fluid, the light benzene separating effect of enhancing light benzene withdrawing can 4, can arrange hydraucone 19 in cooling fluid access tube 5 lower ends.When liquid is flowed through hydraucone 19 from pipeline, because diameter increases, flow velocity can reduce automatically.
The present invention forms eddy current when preventing the discharge opeing of light benzene vent pipe 8 places, causes light benzene outflow resistance to increase, and can on horizontal tank body 17 inwalls at light benzene vent pipe 8 places, vortex shield 22 be set.
Claims (3)
1. the light benzene extraction system of a rich oil negative pressure benzene removal, comprise debenzolizing tower (1), debenzolizing tower (1) top is communicated with light benzene condensate cooler (3) by light benzene steam pipeline (2), it is characterized in that: between light benzene condensate cooler (3) and light benzene return tank (4), by cooling fluid access tube (5) and pressure equalizing pipe (6), be communicated with, light benzene return tank (4) bottom arranges separated flow outlet (7), light benzene return tank (4) is connected with light benzene backflash (9) by light benzene vent pipe (8), light benzene backflash (9) is connected with debenzolizing tower (1) by light benzene return line (10), the upper reflux pump (11) of installing of light benzene return line (10), light benzene return tank (4) top arranges noncondensable gas vent pipe (12), noncondensable gas vent pipe (12) is communicated with shell and tube heat exchanger (13), shell and tube heat exchanger (13) bottom is communicated with light benzene return tank (4) by collector tube (14), upper liquid collecting pump (24) and the electric-control stop valve (26) installed of collector tube (14), negative tube (15) is set on shell and tube heat exchanger (13), negative tube (15) is communicated with vacuum pump (16), liquid collecting pump (24), electric-control stop valve (26) is connected with controller (25) by wire respectively with vacuum pump (16), controller (25) can automatically cut out electric-control stop valve (26) and liquid collecting pump (24) when vacuum pump (16) is worked, when quitting work, automatically opens by vacuum pump (16) electric-control stop valve (26) and liquid collecting pump (24), light benzene return tank (4) comprises horizontal tank body (17), mid-way, horizontal tank body (17) bottom is communicated with the top of vertical tank body (18), horizontal tank body (17) bottom is connected with light benzene vent pipe (8), vertical tank body (18) bottom arranges separated flow outlet (7), horizontal tank body (17) inwall arranges annular brace muscle (21), through hole (23) is offered in annular brace muscle (21) bottom, cooling fluid access tube (5) extends near horizontal tank body (17) bottom in horizontal tank body (17), cooling fluid access tube (5) is separately positioned on vertical tank body (18) both sides with light benzene vent pipe (8), and overflow plate (20) is installed in the horizontal tank body (17) between light benzene vent pipe (8) and vertical tank body (18).
2. the light benzene extraction system of a kind of rich oil negative pressure benzene removal according to claim 1, is characterized in that: cooling fluid access tube (5) lower end arranges hydraucone (19).
3. the light benzene extraction system of a kind of rich oil negative pressure benzene removal according to claim 1, is characterized in that: on horizontal tank body (17) inwall that light benzene vent pipe (8) is located, vortex shield (22) is set.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201210259143.5A CN102796571B (en) | 2012-07-25 | 2012-07-25 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
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| CN201210259143.5A CN102796571B (en) | 2012-07-25 | 2012-07-25 | System for producing light benzene by performing negative pressure debenzolization on rich oil |
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| CN102796571B true CN102796571B (en) | 2014-04-30 |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103160334A (en) * | 2013-03-14 | 2013-06-19 | 济钢集团有限公司 | Method and device for separation of benzene and water in debenzolized rich oil |
| CN105062575B (en) * | 2015-08-03 | 2018-01-16 | 中冶焦耐工程技术有限公司 | Control the technique and device of incoagulable gas continuous-stable discharge in benzene recovery system |
| CN106139626B (en) * | 2016-08-25 | 2018-05-08 | 山东恒利热载体工程技术有限公司 | The online air lift of organic heat carrier removes the technique and device of cracking light component |
| CN115487520B (en) * | 2022-08-31 | 2024-02-13 | 扬州中惠制药有限公司 | Time-sharing definite-throw extraction equipment for various Chinese medicinal materials |
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| CN101544913A (en) * | 2009-05-04 | 2009-09-30 | 济南冶金化工设备有限公司 | Process and equipment for negative pressure benzene removal |
| CN201543262U (en) * | 2009-11-27 | 2010-08-11 | 盂县中信焦化有限公司 | Crude benzene condenser for coking use |
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| CN102408298A (en) * | 2011-09-21 | 2012-04-11 | 宝钢工程技术集团有限公司 | Method of distilling crude benzene by decompression method and device thereof |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100530330B1 (en) * | 2001-11-27 | 2005-11-22 | 주식회사 포스코 | Method for oil separation from cokes oven gas |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101544913A (en) * | 2009-05-04 | 2009-09-30 | 济南冶金化工设备有限公司 | Process and equipment for negative pressure benzene removal |
| CN201543262U (en) * | 2009-11-27 | 2010-08-11 | 盂县中信焦化有限公司 | Crude benzene condenser for coking use |
| CN201603409U (en) * | 2009-12-26 | 2010-10-13 | 太原化工股份有限公司 | Crude benzol reduced pressure distillation device |
| CN102199070A (en) * | 2011-04-06 | 2011-09-28 | 上海同特化工科技有限公司 | Tubular furnace method pressure-reduced debenzolization and distillation process |
| CN102408298A (en) * | 2011-09-21 | 2012-04-11 | 宝钢工程技术集团有限公司 | Method of distilling crude benzene by decompression method and device thereof |
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