CN1008276B - Single tower debenzolizing process and new model of debenzolizing tower - Google Patents
Single tower debenzolizing process and new model of debenzolizing towerInfo
- Publication number
- CN1008276B CN1008276B CN 88105048 CN88105048A CN1008276B CN 1008276 B CN1008276 B CN 1008276B CN 88105048 CN88105048 CN 88105048 CN 88105048 A CN88105048 A CN 88105048A CN 1008276 B CN1008276 B CN 1008276B
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- tower
- oil
- debenzolizing
- benzene
- naphthalene
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Abstract
The present invention relates to a benzene removing technique using a single tower and an apparatus thereof, which belongs to the chemical engineering technique of coking and is widely used for the coal gas purification in a coke-oven plant or a coal gas plant and the like, and the recovery of crude benzene. A novel benzene removing tower is designed, and four qualified products comprising light benzene, refined heavy benzene, naphthalene oil and low-naphthalene lean oil can be obtained simultaneously in the single apparatus. Thereby, the present invention provides a novel benzene removing technique with the advantages of simple technique, short process, little equipment, small occupation of land, low investment, low energy consumption, little sewage, and convenient operation and repair.
Description
The present invention relates to a kind of novel process that reclaims crude benzol, it belongs to the coking chemical technology, can be widely used in the gas purification of coke-oven plant or producer gas plant etc. and the recovery of crude benzol.
In the coke-oven plant or producer gas plant, carry out containing aromatics such as benzene in the low temperature of coal or the coal gas that high temperature carbonization processing is produced.In order to purify coal gas and to reclaim crude benzol, both at home and abroad washing oil that adopt absorb benzene in the coal gas more, remove benzene in the washing oil with steam stripped method again.By retrieval, also there is not single tower to produce the de-benzene process of four kinds of products simultaneously in the world at present.Domestic and international state-of-the-art representative flow process is to adopt two tower de-benzene process of tube furnace heating, and its flow process sees institution of higher learning's didactic works " the coking chemistry product reclaims and processing " P148-150 of the salty prosperous chief editor in Anshan Iron ﹠ Steel College storehouse, the publication of metallurgical industry press for details.
Two tower de-benzene process are benzene washing oil-rich oils containing by the crude benzol washing procedure, after oily vapour interchanger and oily oil heat exchanger make its temperature be increased to 130-140 ℃, enter the dehydration tower flash-evaporation dehydration, send into the tubular oven heating again, send into then and use the open steam stripping in the debenzolizing tower.The temperature of overflowing from the debenzolizing tower top is that 90-93 ℃ crude benzol steam is gone into water-and-oil separator after the condensate cooler cooling, and the crude benzol after the branch water outlet flows into medial launder.The part crude benzol is pumped to the debenzolizing tower top with pump and is refluxed.The naphtalene oil of drawing from the tower side line flows into the naphtalene oil groove certainly.What discharged the debenzolizing tower bottom is hot oil-poor after flowing into poor oil-rich heat exchanger and rich oil heat exchange, send the crude benzol washing procedure to recycle after the water cooler cooling again.
In order to guarantee the circulating washing oil quality, from the rich oil pipeline after the tube furnace heating, draw shallow bid to revivifier and carry out manipulation of regeneration.Use in this to be superheated to 400～450 ℃ direct water vapor through tube furnace and to steam and blow, the washing oil vapour that discharge on the revivifier top enters debenzolizing tower with crude benzol vapour.The residue of regenerator bottoms regularly is disposed to the residue oil groove.
Returning the remaining crude benzol of stream pumps to the further fractionation of two benzene towers from the crude benzol medial launder with pump.Be provided with outer circulation type heater fed heat at the bottom of the tower.The light benzene steam that cat head is overflowed enters the light benzene backflash after condensation cooling, oily water separation.A part refluxes with being pumped to two benzene cats head, and rest part then flowing full is gone into the light benzene medial launder, regularly is sent to the crude benzene refining workshop.The heavy benzene (or refined heavy benzole) that two benzene tower side lines are drawn flows into certainly goes into the heavy benzene medial launder after water-and-oil separator divides water outlet.Discharge naphtalene oil at the bottom of the tower and enter the naphtalene oil groove.There is following urgency problem to be solved in this two towers de-benzene process: (1) native system is except debenzolizing tower, also has one two benzene tower, so increased a whole set of fractionation apparatus (comprising heating, cooling, separation, conveying, backflow, storage etc.), its long flow path, big, the investment height of occupation of land.(2) because equipment is many, also made the Operation and Maintenance complexity, control tower appearred and at the bottom of, cat head oil-feed and throttle (steam) temperature, the problem of regulating aspects such as indirect steam amount, open steam amount, quantity of reflux and inlet amount.(3) owing to the crude benzol that comes out from debenzolizing tower is delivered to the heating of two benzene towers, distillation again after cooling, the light benzene that obtains is also wanted the condensation cooling, is returned stream, has wasted water, electricity, steam widely.(4) because long flow path, generation to contain phenol-cyanogen sewage many, be difficult to handle.
In view of the problem of above-mentioned existence, the objective of the invention is to seek that a kind of technology is simple, flow process is short, equipment is few, occupation of land is little, investment is low, saving energy, sewage are few, the benzene-removing process of convenient operating maintenance.
For realizing this purpose, the measure that the present invention takes is a kind of novel debenzolizing tower of design.This tower is organically combined debenzolizing tower in the original double tower de-benzene process and two benzene towers, finishes the task of two towers with a tower, can directly obtain light benzene, refined heavy benzole, naphtalene oil, the low oil-poor four kinds of qualified product of naphthalene in a tower.
The advantage of single tower debenzolizing process of the present invention is: (1) is because therefore tower generation two towers have saved a whole set of fractionation plant of being made up of nine kinds of 12 equipment.Reduce investment outlay than two tower de-benzene process (refer to 600,000 tons of coke/year scale factory) 710,000 yuan.(2) owing to reduce operating point control, every cover technology can be saved manpower 3 people.(3) single tower takes off benzene and takes off benzene than two towers and save about 40% energy consumption, can economize every year surplus the operational cost 350,000 yuan.
Introduce single tower debenzolizing process of the present invention and novel debenzolizing tower thereof in detail below in conjunction with drawings and Examples.
Fig. 1 is the single tower debenzolizing process schema.
Fig. 2 is novel debenzolizing tower structure iron.
Table 1 is the operating duty of single tower debenzolizing process.
Table 2 is the quality index of single tower debenzolizing process product.
As shown in Figure 1, in the single tower debenzolizing process flow process, (1) oily vapour interchanger and light benzene condensate cooler, (2) oily oil heat exchanger and oil-poor water cooler, (3) tubular oven, (4) revivifier, (5) debenzolizing tower, (6) overhead oil water separator, (7) light benzene water-and-oil separator, (8) light benzene storage tank, (9) light benzene reflux pump, (10) refined heavy benzole water-and-oil separator, (11) refined heavy benzole storage tank, (12) naphtalene oil storage tank, (13) control separator, (14) residue pump.
Rich oil is through oily vapour interchanger (1), oil oil heat exchanger (2) after tubular oven (3) heating, enters debenzolizing tower (5) from stripping section the superiors column plate, open steam enters debenzolizing tower (5) bottom by revivifier (4) and contacts with the rich oil of decline and take off benzene after tube furnace (3) is overheated; The light benzene steam that cat head is overflowed is isolated water of condensation in light benzene water-and-oil separator (7) behind oily vapour interchanger and light benzene condensate cooler (1), the part light benzene is beaten to debenzolizing tower (5) top by light benzene reflux pump (9) and is refluxed, and the rest is product and advances light benzene storage tank (8).Take off hot oil-poor behind the benzene, send the crude benzol washing procedure to recycle behind the oil-poor water cooler (2) through oily oil heat exchanger.
Go up several the 4th～5 layer of tower tray at debenzolizing tower (5), the oil-containing water mixed solution is introduced overhead oil water separator (6), the oil of branch water outlet all returns following one deck tower tray place of debenzolizing tower (5), and water bleeds off; Cut out refined heavy benzole from last several the 14th～20 layer of tower tray, go into refined heavy benzole groove (11) after the branch water outlet in refined heavy benzole water-and-oil separator (10), naphtalene oil cuts out into naphtalene oil groove (12) from last several the 22nd～28 layer of tower tray.Can draw on demand at rectifying section orlop tower tray place and to contain the higher lightweight washing oil of naphthalene.Purpose is for reducing the oil-poor naphthalene that contains.Oil-poor revivifier (4) the water steam stripped of sending into of extension heat goes out washing oil on several the 1st layer of tower tray from descending, and enters debenzolizing tower (5).Discharge residue by revivifier (4) bottom, send outside with pump (14).
To contain benzene washing oil treatment capacity is 45～55m
3The single tower debenzolizing process system of/h is an example, and its operative technique condition is as shown in table 1, and the quality index of its handicraft product is as shown in table 2.
The foregoing description 1 and 2 is Ji steel coking subsidiary factory's single tower debenzolizing process and novel debenzolizing tower actually operating data, and this factory's industrial scale is for producing the medium-sized coke-oven plant of 600,000 tons of metallurgical cokes per year, and the crude benzol washing procedure is handled coal gas amount 28000～32000Nm
3/ h.Debenzolizing tower is handled and is contained benzene washing oil amount 45～55m
3/ h; Debenzolizing tower diameter 1600mm, high 26700mm, the column plate number of plies is 45 layers; Draw oil-water mixture from last several the 5th layer; Draw refined heavy benzole from last several the 15th layer; Draw naphtalene oil from last several the 23rd layer.
For realizing above-mentioned technical process, its key is that the present invention has designed a kind of novel debenzolizing tower, and as shown in Figure 2, the structure of this novel debenzolizing tower is as follows:
(15) tower body, (16) rectifying section, (17) stripping section, (18) diversion plate, (19) garden shape bubble-cap, (20) contain naphthalene lightweight washing oil and draw adjustable plate, (21) refined heavy benzole cuts out mouth, (22) naphtalene oil cuts out mouth, (23) reflux inlet, (24) from the next steam-in of revivifier, (25) rich oil inlet, (26) contain the naphthalene washing oil and cut out mouth, (27) to the oil export of revivifier, (28) oil-poor outlet, (29) light benzene vapour outlet, (30) oil-water mixture outlet.
The whole tower body of debenzolizing tower of the present invention (15) has 45～55 layers of tower tray, and garden shape bubble-cap (19) (except that diversion tower tray and grid tray) is all arranged on every layer of tower tray.The slot opening of bubble-cap is not quite similar on each layer tower tray, is to determine according to the load of the vapour phase in the tower.Full tower is divided into two sections: epimere is rectifying section (16), and hypomere is stripping section (17).Be provided with rich oil inlet (25) on stripping section (17) upper strata; establish dismountable deflector in this inlet; baffle plate is shape in the shape of a spiral; rich oil enters to be tangential direction with tower body; make high temperature go into the tower rich oil and vaporize rapidly also and liquid phase separation, reduce entrainment and avoid erosion corrosion with the protection tower body.Be provided with to contain naphthalene lightweight washing oil outlet (26) and contain naphthalene lightweight washing oil in rectifying section (16) lower floor and draw adjustable plate (20), this adjustable plate is provided with by one deck that the garden shape bubble deck of long-neck riser and one deck grid tray form, and can will contain the naphthalene washing oil and draw or be distributed to equably on the tower tray of stripping section (17) according to the oil-poor naphthalene situation that contains at the bottom of the tower.Go up several the 4th～5 layer of tower tray place at tower body (15) and be provided with diversion plate (18) and oil-water mixture outlet (30), this diversion plate (18) is provided with a plurality of Steam Pipes, pipe is provided with by certain angle, by the guide plate that different directions is arranged, and can make even gas distribution and resistance minimum.Be provided with refined heavy benzole at last several the 14th～20 layer of tower tray place of tower body (15) and cut mouthful (21).Be provided with naphtalene oil at last several 22～28 layers of tower tray place of tower body (15) and cut mouthful (22).Cat head is provided with light benzene reflux inlet (23) and light benzene vapour outlet (29).Be provided with oil export (27) at stripping section (17) orlop to revivifier.Also be provided with the steam-in (24) and the oil-poor outlet (28) that come from revivifier at the bottom of the tower.
The principle of operation and the process of debenzolizing tower of the present invention are as follows:
The stripping section (17) that advances debenzolizing tower from inlet (25) through the rich oil of heating directly contacts on tower tray with the steam of coming in the steam-in (24) from revivifier and carries out steam distillation, and wherein lower boiling benzene class, naphthalene and lightweight washing oil flash to the rectifying section (16) that vapour phase and water vapor are mixed into debenzolizing tower.Be the control quality product, cat head is squeezed into the backflow light benzene from reflux inlet (23), makes the cat head vapor phase temperature maintain 78-79 ℃, certainly will be with water vapor condensation Cheng Shui on the heat exchange tower tray of reflux inlet (23) bottom.For keeping rectifying section (16) thermograde equilibrium, stable,, refined heavy benzole and naphtalene oil are concentrated on a certain tower tray respectively cut out to improve fractionating effect.Oil-water mixture must make it lead to water-and-oil separator with water sepn from oil-containing water mixed solution outlet (30) by the effect of diversion plate (18).Then, oil returns in the tower again.For guaranteeing to obtain low naphthalene washing oil in stripping section (17) bottom, draw adjustable plate (20) with containing naphthalene lightweight washing oil, regulate its whereabouts and control the oil-poor naphthalene amount that contains.
The operating duty of table 1 single tower debenzolizing process
The sequence number project indicator
1 rich oil inlet temperature of stabilizer ℃ 185～195
2 revivifiers oil vapour inlet temperature of stabilizer ℃ 〉=190
3 overhead oil vapor outlet temperature ℃ 78～79
4 diversion line temperature ℃ 94～96
5 refined heavy benzole side stream temperatures ℃ 130～138
6 naphtalene oil side stream temperatures ℃ 155～160
7 superheat steam temperatures ℃ 350～450
8 saturated vapour pressure KPa(kgf/cm
2) 39.2～68.6(4～7)
9 go out the oil-poor temperature of tower ℃ 〉=180
10 tower bottom pressure KPa(kgf/cm
2) 1.77～2.16(0.18～0.22)
11 reflux ratios 3～5
12 open steam specific consumption t steam/t light benzenes 1～1.5
The quality index of table 2 single tower debenzolizing process product
Product quality indicator numerical value
Light density (20 ℃) g/ml 0.872
Benzole forerunning point ℃ 79～80
Do ℃ ≯ 148
Precision (20 ℃) g/ml 0.930～0.98
Heavy initial boiling point ℃ is not less than (normal atmosphere 670mmHg) 160
Quantity of distillate (appearance) % is not less than 85 before 200 ℃ of the benzene
Coumarone-indenes content % is not less than 30
Naphthalene initial boiling point ℃＞180
Quantity of distillate before 210 ℃ (appearance) %＜20
Quantity of distillate before 230 ℃ (appearance) %＞80
Oil does ℃ about 240
Contain naphthalene amount % 〉=45
The poor benzene % 0.4～0.6 that contains
Oil contains naphthalene % 2-5
Claims (5)
1, a kind of single tower debenzolizing process, it comprises by tower body (15), rectifying section (epimere) (16), stripping section (hypomere) (17), diversion plate (18), adjustable plate (20), refined heavy benzole cuts out mouthful (21), naphtalene oil cuts out mouthful (22), reflux inlet (23), rich oil inlet (24), oil-poor outlet (28), the novel debenzolizing tower that light benzene vapour outlet (29) etc. are formed, it is characterized in that after having absorbed the washing oil one rich oil heating of crude benzol in the coal gas, in above-mentioned novel debenzolizing tower, process stripping section (17) directly contacts on tower tray with water vapor and carries out stripping, make lower boiling benzene in the rich oil, naphthalene and lightweight washing oil flash to vapour phase and water vapor mixes, enter rectifying section (16) again, at rectifying section (16) after fractionation, from cat head effusion light benzene steam, cut out refined heavy benzole and naphtalene oil from side line, go out low naphthalene washing oil-oil-poor at the bottom of the tower; Cat head is squeezed into the backflow light benzene, makes the cat head vapor phase temperature maintain 78-79 ℃, by diversion plate (18) oil-water mixture that the tower inner product has is drawn, and regulates by adjustable plate (20) to contain the whereabouts of naphthalene lightweight washing oil to control the oil-poor naphthalene amount that contains.
2, single tower debenzolizing process according to claim 1, the tower body that it is characterized in that debenzolizing tower is made up of 45～55 layers of tower tray that has a garden shape bubble-cap (19).
3, single tower debenzolizing process according to claim 1 and 2, it is characterized in that the diversion plate (18) of debenzolizing tower and last several the 4th～5 layer of tower tray place that oil-water mixture outlet (30) is located at tower, the guide plate that diversion plate (18) is upward arranged by certain angle, different directions by a plurality of riseies and pipe is formed.
4, single tower debenzolizing process according to claim 1 and 2, it is characterized in that the adjustable plate (20) of debenzolizing tower and contain the naphthalene washing oil cutting out the orlop tower tray place that mouthful (26) are located at rectifying section (16), adjustable plate (20) is provided with by one deck that the garden shape bubble deck of long-neck riser and one deck grid tray form.
5, single tower debenzolizing process according to claim 1 is characterized in that the refined heavy benzole of debenzolizing tower cuts out last several 14-20 layer tower tray place that mouthful (21) are located at tower, and naphtalene oil cuts out last several 22-28 layer tower tray place that mouthful (22) are located at tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88105048 CN1008276B (en) | 1988-04-04 | 1988-04-04 | Single tower debenzolizing process and new model of debenzolizing tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88105048 CN1008276B (en) | 1988-04-04 | 1988-04-04 | Single tower debenzolizing process and new model of debenzolizing tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1030070A CN1030070A (en) | 1989-01-04 |
| CN1008276B true CN1008276B (en) | 1990-06-06 |
Family
ID=4833279
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 88105048 Expired CN1008276B (en) | 1988-04-04 | 1988-04-04 | Single tower debenzolizing process and new model of debenzolizing tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1008276B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101270304B (en) * | 2008-05-09 | 2011-01-12 | 攀钢集团钢铁钒钛股份有限公司 | Fine purification technique for coke oven gas |
| CN101302447B (en) * | 2008-05-14 | 2013-04-10 | 莱芜市泰山焦化有限公司 | Method for exchanging changing absorber oil in benzol scrubber when resistance rises in winter |
| CN101544913B (en) * | 2009-05-04 | 2012-06-20 | 济南冶金化工设备有限公司 | Process and equipment for negative pressure benzene removal |
| CN101597517B (en) * | 2009-06-17 | 2012-05-23 | 济钢集团国际工程技术有限公司 | Rich oil de-benzene process |
| CN101879398B (en) * | 2010-06-29 | 2012-06-27 | 南京钢铁股份有限公司 | Recovery process of coking crude benzene dispersing gas and device thereof |
| CN103032679A (en) * | 2011-09-29 | 2013-04-10 | 上海宝钢化工有限公司 | Separation system for reducing vapor-liquid entrainment of vapor phase tube of debenzolization tower |
| CN102776035A (en) * | 2012-07-26 | 2012-11-14 | 黑龙江建龙钢铁有限公司 | Regeneration process method of crude benzene hot lean oil |
| CN102876394B (en) * | 2012-08-24 | 2014-01-22 | 南京钢铁股份有限公司 | Energy-saving method and system for heating coking crude benzene storage tank |
| CN103691142B (en) * | 2012-09-28 | 2016-06-01 | 宝钢工程技术集团有限公司 | Negative pressure regenerating wash oil tower |
-
1988
- 1988-04-04 CN CN 88105048 patent/CN1008276B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN1030070A (en) | 1989-01-04 |
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