CN103382404A - New method for benzene elution of coke-oven gas - Google Patents

New method for benzene elution of coke-oven gas Download PDF

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Publication number
CN103382404A
CN103382404A CN 201310128366 CN201310128366A CN103382404A CN 103382404 A CN103382404 A CN 103382404A CN 201310128366 CN201310128366 CN 201310128366 CN 201310128366 A CN201310128366 A CN 201310128366A CN 103382404 A CN103382404 A CN 103382404A
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benzene
oil
tower
poor
coke
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刘洪涛
张书廷
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BEIJING ZHONGYI FUYOU SCIENCE & TECHNOLOGY Co Ltd
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BEIJING ZHONGYI FUYOU SCIENCE & TECHNOLOGY Co Ltd
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Abstract

The invention relates to a new method for benzene elution of coke-oven gas, including novel structured benzene washing tower and debenzolization tower, a heavy benzol naphthalene oil stripping tower, a steam heating lean oil reboiler, a circulation washing oil regenerator, two integrated crude benzene vapour condensation coolers, two fission lean/rich oil heat exchanger and a vacuum pumping unit. In comparison with a present benzene elution technology of coke-oven gas, crude benzene contained in coal gas after passing through a benzene washing tower can be reduced from 4-5g/Nm<3>(coal gas) to below 0.6g/Nm<3>(coal gas), naphthalene contained in coal gas can be decreased from 200mg/Nm<3>(coal gas) to below 10mg/Nm<3>(coal gas), crude benzene yield can be raised by about 14%, debenzolization energy consumption can be reduced by 40-50%, and oily wastewater will not be produced during the debenzolization process. In short, the new method provided by the invention is beneficial to energy conservation and emission reduction and revenue-enhancing and expenditure control in the coking industry, coking production costs will be obviously reduced, and economic benefit is raised.

Description

About the novel method to coke(oven)gas wash-out benzene
Technical field
The present invention is a kind of relating to the benzene novel method to be taken off in the washing of coke(oven)gas, belongs to energy-saving and water-saving and field of Environment Protection, is mainly used in reclaiming the crude benzol in coke-oven gas and coke(oven)gas is taken off naphthalene purifying.
Background technology
At present, China's coal chemical enterprise, for coke oven air purge benzene, coal gas is washed benzene Ta Neichang and is loaded ceramic packing and metallurgic orifice corrugated packing; For the benzene that takes off of washing the benzene rich oil, often adopt gas pipe type furnace heating rich oil, board-like single tower or double tower atmospheric steam to carry and heat up in a steamer explained hereafter crude benzol or light benzene.Existing wash-out benzene process Main Problems: the one,, wash that coal gas contains benzene after the benzene tower, it is high to contain naphthalene; The 2nd,, rich oil de-benzene process energy consumption is high, the water consumption is large, waste water is many; The 3rd,, oil washing consumption is high, and the crude benzol yield is low, deficiency in economic performance.Recently, indivedual coal chemical enterprises are arranged, adopt negative pressure benzene removal for washing the benzene rich oil; This measure although obviously reduced the superheated vapour amount that passes into debenzolizing tower, has reduced and has taken off benzene cooling-water consumption and wastewater flow rate, and other problem still exists.The present invention is intended to overcome the problems and shortcomings that existing coke(oven)gas wash-out benzene process exists, for the coking industry energy-saving and emission-reduction, increase income and economize on spending, increase economic efficiency significant.
Summary of the invention
The present invention, be a kind of novel method to coke(oven)gas wash-out benzene, wash benzene tower and debenzolizing tower, heavy benzol naphtalene oil by novel texture and carry and heat up in a steamer tower, the oil-poor reboiler of steam heating, circulating washing oil revivifier, two sections one crude benzene steam condensing water coolers, two sections split poor oil-rich heat exchangers and vacuum unit and form.Main summary of the invention is as follows:
1, being provided with the oil-poor reboiler of gravity flow at the bottom of debenzolizing tower, taking off the required heat of benzene, is mainly to utilize middle pressure steam to pass through the oil-poor supply of reboiler indirect heating, does not pass into overheated steam in revivifier and debenzolizing tower, and adopts the vacuum distilling operation.
2, utilize two sections higher phlegmas of crude benzol condensate cooler epimere temperature, push up to debenzolizing tower and play thermal backflow.
If 3 produce crude benzol, the debenzolizing tower rectifying section is not established naphtalene oil extraction side line, if produce light benzene and heavy benzol fraction of naphthalene oil, the debenzolizing tower rectifying section is provided with heavy benzol fraction of naphthalene oil extraction side line, the heavy benzol fraction of naphthalene oil of extraction will heat up in a steamer tower and steams the light benzene component by carrying, and returns to the debenzolizing tower rectifying section.
4, temperature is lower wash the benzene rich oil and temperature higher take off the oil-poor heat exchange of benzene, be divided into two sections: after first paragraph is placed on oil-poor pump, before second segment is placed on oil-poor pump.
5, wash the benzene tower, in be filled with multistage metal rhombus net corrugated regular filler.Debenzolizing tower is comprised of three sections of upper, middle and lowers, the epimere diameter is less, the corrugated metal structured packing of aperture rhombus net is equipped with in inside, the stage casing diameter is larger, the corrugated metal structured packing of macropore rhombus net is equipped with in inside, be provided with the disconnected tower tray of oil-poor collection between stage casing and hypomere, hypomere is equipped with some with the oil-poor vaporization flash distillation plate of sieve aperture.
6, two sections crude benzol condensate coolers, establish the condensed fluid collection dish between two sections.
7, the gas temperature that advances to wash the benzene tower is controlled in 20~23 ℃ of scopes, and the oil-poor temperature of advancing to wash the benzene tower is controlled in 22~25 ℃ of scopes, and the rich oil temperature of advancing debenzolizing tower is controlled at 160 ℃, and the oil-poor temperature that goes out debenzolizing tower is controlled at 180 ℃ of left and right; When producing crude benzol, debenzolizing tower top temperature is controlled at 108 ℃ of left and right, crude benzol condensate cooler epimere outlet crude benzene vapor temperature is controlled at 65 ℃ of left and right, and crude benzol condensate cooler hypomere outlet crude benzol temperature is controlled at below 20 ℃, and the debenzolizing tower pressure on top surface is controlled at the 82mmHg left and right.
The present invention, compare with existing coke(oven)gas wash-out benzene process method, washing after the benzene tower coal gas contains crude benzol and can be dropped to below 0.6g/Nm3 (coal gas) by 4~5g/Nm3 (coal gas), coal gas contains naphthalene and can be dropped to below 10mg/Nm3 (coal gas) by 200mg/Nm3 (coal gas), the crude benzol yield can improve 14% left and right, take off the benzene energy consumption and can reduce by 40~50%, take off the benzene process and do not produce oily(waste)water.In a word, the present invention is conducive to the coking industry energy-saving and emission-reduction and increases income and economizes on spending, and can obviously reduce the coking production cost and increase economic efficiency.
Description of drawings
Fig. 1 is the process flow diagram of example 1 of the present invention;
Fig. 2 is the process flow diagram of example 2 of the present invention;
Shown in figure:
C-01 washes the benzene tower, the C-02 debenzolizing tower, C-03 heavy benzol naphtalene oil is carried and is heated up in a steamer tower, E-01 circulating washing oil revivifier, the oil-poor reboiler of E-02, E-03 rich oil well heater, E-04 oil-poor with one section interchanger of rich oil, E-05 oil-poor with two sections interchanger of rich oil, the oil-poor one section water cooler of E-06, the oil-poor two-step cooling device of E-07, E-08 crude benzol condensate cooler, E-09 heavy benzol naphtalene oil reboiler, T-01 washes benzene rich oil groove, T-02 takes off the benzene backflash, T-03 crude benzol or light benzene product medial launder, T-04 vacuum buffer groove, P-01 rich oil pump, the oil-poor pump of P-02, P-03 takes off the benzene reflux pump, P-04 crude benzol or light benzene product pump, P-05 regenerating wash oil residue pump, the P-06 vacuum pump.
Embodiment
The present invention will be further described below in conjunction with embodiment:
Embodiment 1:(washes benzene rich oil de-benzene process, is that single tower is produced crude benzol technique without the naphtalene oil side line)
Wash the rich oil of benzene tower from C-01, through T-01 rich oil groove, extract out with P-01 rich oil pump, pass through successively E-05 oil-poor with two sections interchanger of rich oil, E-04 is oil-poor and one section interchanger of rich oil, E-03 rich oil well heater, the rich oil temperature is heated to 160 ℃ of left and right, sends in debenzolizing tower between C-02 debenzolizing tower rectifying section and stripping section.At the debenzolizing tower stripping section, hot rich oil contacts with oil-poor steam counter-flow from the debenzolizing tower flash zone, and the light constituents such as the crude benzol in rich oil, naphthalene are carried to be heated up in a steamer in vapour phase, and enters into the rectifying section of debenzolizing tower.The temperature of overflowing from debenzolizing tower top is the oily vapour of 108 ℃ of left and right approximately, and is cooling through the E-08 fractional condensation; The first step, at the epimere of E-08 crude benzol condensate cooler, crude benzene vapor is cooled to approximately 65 ℃, and the phlegma that consequent temperature is higher through the liquid collecting dish, certainly flows into T-02 and takes off the benzene backflash, then return stream by the P-03 pump to debenzolizing tower; Second step, at E-08 crude benzol condensate cooler hypomere, will be from the about non-condensable gas of 65 ℃ of the temperature of E-08 epimere, full coalescence is cooled to below 20 ℃, as the crude benzol product, flows automatically to T-03 crude benzol product medial launder, then sends outside with the extraction of P-04 crude benzol product pump.The bleeder of T-03 crude benzol product medial launder is connected with T-04 vacuum buffer groove, and the T-04 groove is connected with the P-06 vacuum pump, guarantees to take off benzene series system vacuum tightness and meets the requirements.At the debenzolizing tower stripping section, after washing the benzene rich oil and oil-poor steam counter-flow from flash zone contacting, can flow automatically to and become on disconnected tower tray that to take off benzene oil-poor.It is oil-poor that major part is taken off benzene, pass through the E-02 reboiler by disconnected tower tray gravity flow, utilize oil-poor after steam heating, flow automatically to again the debenzolizing tower flash zone, the oil-poor steam that flashes off thus, enter the debenzolizing tower stripping section by disconnected tower tray, with from the stripping section top wash benzene rich oil counter current contact, it is carried heating up in a steamer takes off benzene.It is oil-poor that sub-fraction is taken off benzene, and from flowing in E-01 circulating washing oil revivifier, its Residual oil of regenerating is sent outside by P-05 regenerating wash oil residue pump by the section tower tray; And utilize middle pressure steam indirect heating regeneration Residual oil, from the regenerating wash oil gas that E-01 overflows, be imported into bottom the debenzolizing tower flash zone.Utilization by E-03 rich oil well heater, will be heated to 160 ℃ of left and right from the indirect heating exhaust steam that E-01 discharges from the benzene rich oil of washing of E-04.Approximately 180 ℃ of left and right of discharging at the bottom of the debenzolizing tower flash zone hot oil-poor, pass through successively E-04 oil-poor with one section interchanger of rich oil, the oil-poor transferpump of P-02, E-05 is oil-poor and two sections interchanger of rich oil, the oil-poor one section water cooler of E-06, the oil-poor two-step cooling device of E-07, being cooled is controlled in 22~25 ℃ of scopes, finally is sent to C-01 and washes benzene tower internal recycle and wash benzene.In the gas final cold operation, to not take off the benzene gas temperature is controlled in 20~23 ℃ of scopes, send into C-01 and wash the benzene tower, in this tower, coal gas with wash the oil-poor counter current contact of benzene, crude benzol in Poor oil absorbing coal gas and naphthalene component become again and wash the benzene rich oil, then are sent to steam heating vacuum distilling and take off benzene series system and carry out multiple steaming.Need emphasize: embodiment 1, and it is oil-poor that benzene is taken off in utilization, when coal gas is washed benzene, also removed the naphthalene component in coal gas; When washing the benzene rich oil de-benzene, allow the naphthalene component take out of with the crude benzol product, the debenzolizing tower rectifying section is not established naphtalene oil extraction side line.
Embodiment 2:(washes benzene rich oil de-benzene process, is that the major-minor double tower is produced light benzene and heavy benzol naphtalene oil mixed fraction technique.King-tower is the C-02 debenzolizing tower, secondary tower be C-03 heavy benzol naphtalene oil carry heat up in a steamer tower)
Embodiment 2, having set up C-03 heavy benzol naphtalene oil carries and heats up in a steamer tower and E-09 heavy benzol naphtalene oil reboiler, in C-02 debenzolizing tower rectifying section appropriate location, be provided with heavy benzol naphtalene oil extraction side line, the heavy benzol naphtalene oil mixed fraction of extraction, contain the light benzene component thus, carry by C-03 and heat up in a steamer tower, light constituent in the heavy benzol fraction of naphthalene oil is carried distillating come, then return to C-02 debenzolizing tower rectifying section.Carry and heat up in a steamer the needed heat of tower, utilize steam to pass through E-09 heavy benzol naphtalene oil reboiler indirect heating and supply with.Debenzolizing tower top effusion oil gas, cooling through the E-08 fractional condensation, produce the light benzene product.Other processes and embodiment 1 are identical.

Claims (10)

1. novel method for coke(oven)gas wash-out benzene is characterized in that: carry and heat up in a steamer tower, oil-poor reboiler, circulating washing oil revivifier, two sections one crude benzene steam condensing water coolers, two sections split poor oil-rich heat exchangers and vacuum unit and form by washing benzene tower and debenzolizing tower, heavy benzol naphtalene oil.
2. the novel method of coke(oven)gas wash-out benzene as described in right 1, it is characterized in that: being provided with the oil-poor reboiler of gravity flow at the bottom of debenzolizing tower, taking off the required heat of benzene, is mainly to utilize middle pressure steam to pass through the oil-poor supply of reboiler indirect heating, and adopts the vacuum distilling operation.
3. the novel method of coke(oven)gas wash-out benzene as described in right 1, is characterized in that: utilize two sections higher phlegmas of crude benzol condensate cooler epimere temperature, push up to debenzolizing tower and play thermal backflow.
4. the novel method of coke(oven)gas wash-out benzene as described in right 1 is characterized in that: produce crude benzol, the debenzolizing tower rectifying section is not established naphtalene oil extraction side line.
5. the novel method of coke(oven)gas wash-out benzene as described in right 1, it is characterized in that: produce light benzene and heavy benzol fraction of naphthalene oil, the debenzolizing tower rectifying section is provided with heavy benzol fraction of naphthalene oil extraction side line, the heavy benzol fraction of naphthalene oil of extraction, to heat up in a steamer tower and steam the light benzene component by carrying, and return to the debenzolizing tower rectifying section, to produce light benzene and heavy benzol fraction of naphthalene oil.
6. the novel method of coke(oven)gas wash-out benzene as described in right 1 is characterized in that: temperature is lower wash the benzene rich oil and temperature higher take off the oil-poor heat exchange of benzene, be divided into two sections, before first paragraph is placed on oil-poor pump, after second segment is placed on oil-poor pump.
7. the novel method of coke(oven)gas wash-out benzene as described in right 1, is characterized in that: wash benzene Ta Tanei and be filled with multistage metal rhombus net corrugated regular filler.
8. the novel method of coke(oven)gas wash-out benzene as described in right 1, it is characterized in that: debenzolizing tower is comprised of three sections of upper, middle and lowers, the epimere diameter is less, the corrugated metal structured packing of aperture rhombus net is equipped with in inside, the stage casing diameter is larger, large empty rhombus net corrugated metal structured packing is equipped with in inside, is provided with the disconnected tower tray of oil-poor collection between stage casing and hypomere, and hypomere is equipped with some with the oil-poor vaporization flash distillation plate of sieve aperture.
9. the novel method of coke(oven)gas wash-out benzene as described in right 1, is characterized in that: establish the disconnected tower tray of condensed fluid collection between two sections of two sections crude benzol condensate coolers.
10. the novel method of coke(oven)gas wash-out benzene as described in right 1, it is characterized in that: the gas temperature that advances to wash the benzene tower is controlled in 20~23 ℃ of scopes, the oil-poor temperature of advancing to wash the benzene tower is controlled in 22~25 ℃ of scopes, the rich oil temperature of advancing debenzolizing tower is controlled at 160 ℃, the oil-poor temperature that goes out debenzolizing tower is controlled at 180 ℃ of left and right, debenzolizing tower top temperature is controlled at 108 ℃ of left and right, crude benzol condensate cooler epimere outlet crude benzene vapor temperature is controlled at 65 ℃ of left and right, crude benzol condensate cooler hypomere outlet crude benzol temperature is controlled at below 20 ℃, the debenzolizing tower pressure on top surface is controlled at the 82mmHg left and right.
CN 201310128366 2013-04-15 2013-04-15 New method for benzene elution of coke-oven gas Pending CN103382404A (en)

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
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
CN104789273A (en) * 2015-03-27 2015-07-22 山东钢铁股份有限公司 System for recycling coke oven raw-gas benzene substances by using raw-gas waste heat
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
CN107890684A (en) * 2017-12-22 2018-04-10 中冶焦耐(大连)工程技术有限公司 A kind of reboiler method negative pressure crude benzol Distallation systm
CN108096999A (en) * 2017-12-22 2018-06-01 中冶焦耐(大连)工程技术有限公司 A kind of reboiler method negative pressure crude benzol distillation technique

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
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
CN104789273A (en) * 2015-03-27 2015-07-22 山东钢铁股份有限公司 System for recycling coke oven raw-gas benzene substances by using raw-gas waste heat
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
CN107890684A (en) * 2017-12-22 2018-04-10 中冶焦耐(大连)工程技术有限公司 A kind of reboiler method negative pressure crude benzol Distallation systm
CN108096999A (en) * 2017-12-22 2018-06-01 中冶焦耐(大连)工程技术有限公司 A kind of reboiler method negative pressure crude benzol distillation technique
CN107890684B (en) * 2017-12-22 2023-06-16 中冶焦耐(大连)工程技术有限公司 Reboiler method negative pressure crude benzol distillation system
CN108096999B (en) * 2017-12-22 2023-06-20 中冶焦耐(大连)工程技术有限公司 Reboiler method negative pressure crude benzene distillation process

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