CN108096999A - A kind of reboiler method negative pressure crude benzol distillation technique - Google Patents
A kind of reboiler method negative pressure crude benzol distillation technique Download PDFInfo
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- CN108096999A CN108096999A CN201711401506.3A CN201711401506A CN108096999A CN 108096999 A CN108096999 A CN 108096999A CN 201711401506 A CN201711401506 A CN 201711401506A CN 108096999 A CN108096999 A CN 108096999A
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- oil
- crude benzol
- debenzolizing tower
- benzene
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7027—Aromatic hydrocarbons
Abstract
The present invention relates to a kind of reboiler method negative pressure crude benzol distillation techniques, provide heat source for debenzolizing tower using superheated steam heating tower's bottoming cycle washing oil, under certain vacuum degree, make to distill out crude benzol or light benzene in washing oil in debenzolizing tower.In order to keep circulating washing oil quality, the circulating washing oil for drawing 1~1.5% is sent into the regenerator with certain vacuum degree, and heating regeneration is carried out using superheated steam；Naphtalene oil fraction is drawn in debenzolizing tower side line, to reduce oil-poor amount containing naphthalene.Compared with existing crude benzol distillation technique, the present invention has the remarkable advantages such as operating cost is low, environment protecting is good.
Description
Technical field
The present invention relates to coking chemical Product recycling technical field more particularly to a kind of reboiler method negative pressure crude benzol distillation works
Skill.
Background technology
To reduce discharge of wastewater, recent coking industry occurs that (steam does not participate in directly without steaming process crude benzol distillation technique
Distillation process), this technique is to use diamond heating rich oil and cycling hot oil-poor, the technique that heat is provided for debenzolizing tower, the work
Crude benzol separation water is seldom during skill, greatly reduces the discharge of waste water.But tube furnace generates substantial amounts of exhaust gas and but causes
Certain exhaust gas discharge；The tubular type furnace exhaust heated simultaneously using coke-stove gas is difficult to meet coking chemistry industrial pollutants to arrange
Put standard, it is necessary to have mating emission-control equipment, investment cost is higher；Although it can be dropped using the tube furnace of BF gas heating
SO in low exhaust gas2Content, but equipment is larger, and generation exhausted air quantity is more, and environment protecting is poor.Meanwhile using diamond heating rich oil and
Washing oil can cause a large amount of cohesions, the coking of rich oil and washing oil, generate substantial amounts of residue oil, cause the waste of washing oil, operating cost
It is high.
In conclusion at this stage without steaming process crude benzol distillation technique in operating cost, environmental protection etc. existing defects, it is anxious
It is to be solved.
For current coking industry extinguishing technique mostly using dry coke quenching technique, which generates substantial amounts of high pressure superheater
Steam, this steam are usually used in generating electricity or be used in gas purification process.The present invention is the hyperthermia and superheating generated using dry coke quenching
Steam heats the negative pressure crude benzol distillation technique of rich oil and washing oil.
The content of the invention
The present invention provides a kind of reboiler method negative pressure crude benzol distillation techniques, compared with existing crude benzol distillation technique, tool
There are the remarkable advantages such as operating cost is low, environment protecting is good.
In order to achieve the above object, the present invention is realized using following technical scheme：
A kind of reboiler method negative pressure crude benzol distillation technique, including：
1) poor oil-rich heat exchanger is sent into from the washing oil washed in benzene column absorption coal gas after benezene material, it is poor by heat with debenzolizing tower bottom
Into rich oil heater after 210~245 DEG C of oil-poor heat exchange of heat that oil pump is drawn, debenzolizing tower is entered after being heated to 190~220 DEG C；
The oil-poor final cooling zone that is sent to again after oil-poor one-step cooling device and oil-poor cooler two-step cooling after heat exchange is used to wash benzene；
2) in debenzolizing tower, stripped, distilled under the vacuum degree of -40~-70KPa, a part is produced from debenzolizing tower bottom
Circulating washing oil is sent to reboiler, after 300~550 DEG C of high pressure superheated steams heating come using dry quenching system, returns again to de- benzene
Tower, as the heat source of crude benzol distillation and stripping component；
3) 55~70 DEG C of crude benzene vapors or light benzene steam of debenzolizing tower tower top effusion, after crude benzol or light benzene condensate cooler
It is separated into crude benzol or light benzene backflash, the incoagulable gas after separation is after benzene vapour cooler further cooling, with de-
Benzene vacuum pump or injector are sent into coal gas system；Liquid after separation carries out water-oil separating in crude benzol or light benzene backflash, uses
Crude benzol or light benzene pump send the crude benzol isolated of a part or light benzene to debenzolizing tower tower top as flowing back, remaining as product outside
It send；
4) naphtalene oil fraction is drawn in debenzolizing tower side line, to reduce oil-poor amount containing naphthalene；The naphtalene oil fraction of extraction enters residue slot,
Periodically sent outside with pump；
5) to keep circulating washing oil quality, the circulating washing oil for drawing 1%~1.5% is sent into regenerator, 200~230
DEG C, carry out distillation regeneration under the vacuum degree of -75~-95KPa, regeneration heat source is the high temperature super heated steam from dry quenching system；
6) the regeneration residue at debenzolizing tower bottom is discharged into residue slot, is periodically sent outside with pump；The incoagulable gas at debenzolizing tower bottom is through washing
After oily condensate cooler, fuel and vapor separator and the cooling of oil and gas cooler, sent with regenerative vacuum pump or injector to coal gas system；
During above system is run, the operating pressure subatmospheric of debenzolizing tower and regenerator, i.e., in negative pressure state.
To ensure the efficiency of crude benzol distillation in debenzolizing tower, debenzolizing tower operating pressure is taken out with de- benzene vacuum pumping or injector
To 30~60KPa of absolute pressure, debenzolizing tower bottom operation temperature maintains 190~245 DEG C.
To ensure the efficiency of regenerating wash oil in regenerator, regenerator operation pressure with regenerative vacuum pump is taken out or injector is taken out
5~25KPa of absolute pressure, operation temperature maintain 200~230 DEG C.
To reduce debenzolizing tower resistance, for the rectifying section of debenzolizing tower using tray structure, profit reduction and reserving section uses filling-material structure.
The condensation water generated after high pressure superheated steam heat exchange generates low-pressure steam by flashing, and is sent to low-pressure steam pipe network
It recycles, remaining condensation water returns to boiler and recycles.
Compared with prior art, the beneficial effects of the invention are as follows：
1) operating cost is low：Compared with existing no steaming process negative pressure crude benzol distillation technique, the present invention is rich using steam heating
Oil and washing oil, operation temperature is low, has effectively contained the slagging of washing oil, reduces the renewal amount of residue oil output and washing oil, drop
Low operating cost；
2) environment protecting is good：Compared with existing crude benzol distillation technique, the present invention is not provided with tube furnace, will not generate tube furnace
Exhaust gas reduces discharge amount of exhaust gas；Meanwhile crude benzol of the present invention separation water yield is seldom, greatly reduces wastewater displacement；
3) debenzolizing tower, regenerator top are separated benzene vapour, oil gas etc. are sent to coal gas system, ensure that the feature of environmental protection of technique
And effective recycling of benezene material.
Description of the drawings
Fig. 1 is a kind of flow chart of reboiler method negative pressure crude benzol distillation technique of the present invention.
In figure：1. 2. regenerator of debenzolizing tower, 3. reboiler, 4. crude benzol or 5. crude benzol of light benzene condensate cooler or light benzene return
6. benzene vapour cooler 7. of chute takes off 10. oil gas of benzene vacuum pump or 8. washing oil condensate cooler of injector, 9. fuel and vapor separator
11. regenerative vacuum pump of cooler or 12. crude benzol of injector or light benzene pump 13. heat, 14. poor oil-rich heat exchangers 15. of oil-poor pump
Oil-poor 16. oil-poor 17. rich oil heater of two-step cooling device of one-step cooling device
Specific embodiment
The specific embodiment of the present invention is described further below in conjunction with the accompanying drawings：
As shown in Figure 1, a kind of reboiler method negative pressure crude benzol distillation technique of the present invention, including：
1) poor oil-rich heat exchanger 14 is sent into from the washing oil washed in benzene column absorption coal gas after benezene material, with debenzolizing tower bottom by heat
Into rich oil heater 17 after 210~245 DEG C of oil-poor heat exchange of heat that oil-poor pump 13 is drawn, into de- after being heated to 190~220 DEG C
Benzene column 1；After heat exchange it is oil-poor again through oil-poor one-step cooling device 15 and oil-poor two-step cooling device 16 cooling after be sent to final cooling zone use
In washing benzene；
2) in debenzolizing tower 1, stripped, distilled under the vacuum degree of -40~-70KPa, a part is produced from debenzolizing tower bottom
Circulating washing oil is sent to reboiler 3, after 300~550 DEG C of high pressure superheated steams heating come using dry quenching system, returns again to de- benzene
Tower 1, as the heat source of crude benzol distillation and stripping component；
3) 55~70 DEG C of crude benzene vapors or light benzene steam of 1 tower top of debenzolizing tower effusion, through crude benzol or light benzene condensate cooler 4
Separated afterwards into crude benzol or light benzene backflash 5, the incoagulable gas after separation after benzene vapour cooler 6 further cooling,
Coal gas system is sent into de- benzene vacuum pump or injector 7；Liquid after separation carries out grease point in crude benzol or light benzene backflash 5
From the crude benzol isolated of a part or light benzene being sent to 1 tower top of debenzolizing tower as flowing back by the use of crude benzol or light benzene pump 12, remaining conduct
Product is sent outside；
4) naphtalene oil fraction is drawn in debenzolizing tower side line, to reduce oil-poor amount containing naphthalene；The naphtalene oil fraction of extraction enters residue slot,
Periodically sent outside with pump；
5) to keep circulating washing oil quality, the circulating washing oil for drawing 1%~1.5% is sent into regenerator 2,200~230
DEG C, carry out distillation regeneration under the vacuum degree of -75~-95KPa, regeneration heat source is the high temperature super heated steam from dry quenching system；
6) the regeneration residue at debenzolizing tower bottom is discharged into residue slot, is periodically sent outside with pump；The incoagulable gas at debenzolizing tower bottom is through washing
After oily condensate cooler 8, fuel and vapor separator 9 and oil and gas cooler 10 cool down, sent with regenerative vacuum pump or injector 11 to coal gas
System；
During above system is run, the operating pressure subatmospheric of debenzolizing tower 1 and regenerator 2, i.e., in negative pressure state.
To ensure the efficiency of crude benzol distillation in debenzolizing tower 1, by debenzolizing tower operating pressure de- benzene vacuum pumping or injector 7
30~60KPa of absolute pressure is evacuated to, debenzolizing tower bottom operation temperature maintains 190~245 DEG C.
To ensure the efficiency of regenerating wash oil in regenerator 2, by regenerator operation pressure regenerative vacuum pump pumping or injector
11 take out 5~25KPa of absolute pressure, and operation temperature maintains 200~230 DEG C.
To reduce by 1 resistance of debenzolizing tower, for the rectifying section of debenzolizing tower 1 using tray structure, profit reduction and reserving section uses filling-material structure.
The condensation water generated after high pressure superheated steam heat exchange generates low-pressure steam by flashing, and is sent to low-pressure steam pipe network
It recycles, remaining condensation water returns to boiler and recycles.
A kind of operation principle of reboiler method negative pressure crude benzol distillation technique of the present invention is to use superheated steam heating tower
Bottoming cycle washing oil provides heat source for debenzolizing tower 1, under certain vacuum degree, make to distill out in debenzolizing tower 1 crude benzol in washing oil or
The technical process of light benzene.In order to keep circulating washing oil quality, the circulating washing oil for drawing 1~1.5% is sent into certain vacuum degree
Regenerator 2 in, carry out heating regeneration using superheated steam；Naphtalene oil fraction is drawn in debenzolizing tower side line, it is oil-poor containing naphthalene to reduce
Amount.The technique has the remarkable advantages such as operating cost is low, environment protecting is good.
The foregoing is only a preferred embodiment of the present invention, but protection scope of the present invention be not limited thereto,
Any one skilled in the art in the technical scope disclosed by the present invention, technique according to the invention scheme and its
Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.
Claims (5)
1. a kind of reboiler method negative pressure crude benzol distillation technique, which is characterized in that including：
1) poor oil-rich heat exchanger is sent into from the washing oil washed in benzene column absorption coal gas after benezene material, with debenzolizing tower bottom by the oil-poor pump of heat
Into rich oil heater after 210~245 DEG C of oil-poor heat exchange of heat drawn, debenzolizing tower is entered after being heated to 190~220 DEG C；After heat exchange
Oil-poor be sent to final cooling zone after oil-poor one-step cooling device and the cooling of oil-poor two-step cooling device for washing benzene again；
2) in debenzolizing tower, stripped, distilled under the vacuum degree of -40~-70KPa, part Xun Huan is produced from debenzolizing tower bottom
Washing oil is sent to reboiler, after 300~550 DEG C of high pressure superheated steams heating come using dry quenching system, returns again to debenzolizing tower, makees
For the heat source of crude benzol distillation and stripping component；
3) 55~70 DEG C of crude benzene vapors or light benzene steam of debenzolizing tower tower top effusion, enter after crude benzol or light benzene condensate cooler
Crude benzol or light benzene backflash are separated, and the incoagulable gas after separation is true with de- benzene after benzene vapour cooler further cooling
Sky pump or injector are sent into coal gas system；Liquid after separation carries out water-oil separating in crude benzol or light benzene backflash, uses crude benzol
Or light benzene pump send a part of crude benzol isolated or light benzene to debenzolizing tower tower top as reflux, remaining sends outside as product；
4) naphtalene oil fraction is drawn in debenzolizing tower side line, to reduce oil-poor amount containing naphthalene；The naphtalene oil fraction of extraction enters residue slot, periodically
It is sent outside with pump；
5) for keep circulating washing oil quality, draw 1%~1.5% circulating washing oil be sent into regenerator in, 200~230 DEG C ,-
Distillation regeneration is carried out under the vacuum degree of 75~-95KPa, regeneration heat source is the high temperature super heated steam from dry quenching system；
6) the regeneration residue at debenzolizing tower bottom is discharged into residue slot, is periodically sent outside with pump；The incoagulable gas at debenzolizing tower bottom is cold through washing oil
After solidifying cooler, fuel and vapor separator and the cooling of oil and gas cooler, sent with regenerative vacuum pump or injector to coal gas system；
During above system is run, the operating pressure subatmospheric of debenzolizing tower and regenerator, i.e., in negative pressure state.
2. a kind of reboiler method negative pressure crude benzol distillation technique according to claim 1, which is characterized in that ensure debenzolizing tower
The efficiency of interior crude benzol distillation, 30~60KPa of absolute pressure is evacuated to by debenzolizing tower operating pressure with de- benzene vacuum pumping or injector,
Debenzolizing tower bottom operation temperature maintains 190~245 DEG C.
3. a kind of reboiler method negative pressure crude benzol distillation technique according to claim 1, which is characterized in that ensure regenerator
Regenerator operation pressure with regenerative vacuum pump is taken out or injector takes out 5~25KPa of absolute pressure, behaviour by the efficiency of interior regenerating wash oil
200~230 DEG C are maintained as temperature.
4. a kind of reboiler method negative pressure crude benzol distillation technique according to claim 1, which is characterized in that reduce debenzolizing tower
Resistance, for the rectifying section of debenzolizing tower using tray structure, profit reduction and reserving section uses filling-material structure.
A kind of 5. reboiler method negative pressure crude benzol distillation technique according to claim 1, which is characterized in that high pressure superheated steam
The condensation water generated after heat exchange generates low-pressure steam by flashing, and is sent to low-pressure steam pipe network recycling, and remaining condensation water returns
Back boiler recycles.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201711401506.3A CN108096999B (en) | 2017-12-22 | 2017-12-22 | Reboiler method negative pressure crude benzene distillation process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711401506.3A CN108096999B (en) | 2017-12-22 | 2017-12-22 | Reboiler method negative pressure crude benzene distillation process |
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| CN108096999A true CN108096999A (en) | 2018-06-01 |
| CN108096999B CN108096999B (en) | 2023-06-20 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108911938A (en) * | 2018-08-22 | 2018-11-30 | 樊晓光 | In in a kind of crude benzol Distallation systm, low-pressure steam heating process and device |
| CN111253203A (en) * | 2020-03-17 | 2020-06-09 | 本钢板材股份有限公司 | Heat exchange optimization process for crude benzene distillation section |
| CN111939584A (en) * | 2020-09-04 | 2020-11-17 | 中冶焦耐(大连)工程技术有限公司 | Process and system for evaporating crude benzene in benzene hydrogenation reaction system |
| CN113150840A (en) * | 2021-04-23 | 2021-07-23 | 济南冶金化工设备有限公司 | Self-azeotropic negative pressure debenzolization process |
| CN113521965A (en) * | 2021-01-29 | 2021-10-22 | 乌海宝杰新能源材料有限公司 | Efficient and energy-saving granulation tail gas treatment system and treatment process thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289633A (en) * | 2007-04-20 | 2008-10-22 | 宝山钢铁股份有限公司 | Novel regeneration process for circulation oil of crude benzol device |
| CN103382404A (en) * | 2013-04-15 | 2013-11-06 | 北京中亿孚佑科技有限公司 | New method for benzene elution of coke-oven gas |
| CN103555377A (en) * | 2013-10-24 | 2014-02-05 | 天津市创举科技有限公司 | Method and equipment for reduced-pressure benzene removal |
-
2017
- 2017-12-22 CN CN201711401506.3A patent/CN108096999B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289633A (en) * | 2007-04-20 | 2008-10-22 | 宝山钢铁股份有限公司 | Novel regeneration process for circulation oil of crude benzol device |
| CN103382404A (en) * | 2013-04-15 | 2013-11-06 | 北京中亿孚佑科技有限公司 | New method for benzene elution of coke-oven gas |
| CN103555377A (en) * | 2013-10-24 | 2014-02-05 | 天津市创举科技有限公司 | Method and equipment for reduced-pressure benzene removal |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108911938A (en) * | 2018-08-22 | 2018-11-30 | 樊晓光 | In in a kind of crude benzol Distallation systm, low-pressure steam heating process and device |
| CN108911938B (en) * | 2018-08-22 | 2024-01-23 | 樊晓光 | Middle-low pressure steam heating process and device in crude benzene distillation system |
| CN111253203A (en) * | 2020-03-17 | 2020-06-09 | 本钢板材股份有限公司 | Heat exchange optimization process for crude benzene distillation section |
| CN111939584A (en) * | 2020-09-04 | 2020-11-17 | 中冶焦耐(大连)工程技术有限公司 | Process and system for evaporating crude benzene in benzene hydrogenation reaction system |
| CN111939584B (en) * | 2020-09-04 | 2023-09-15 | 中冶焦耐(大连)工程技术有限公司 | Crude benzene evaporation process and system in benzene hydrogenation reaction system |
| CN113521965A (en) * | 2021-01-29 | 2021-10-22 | 乌海宝杰新能源材料有限公司 | Efficient and energy-saving granulation tail gas treatment system and treatment process thereof |
| CN113150840A (en) * | 2021-04-23 | 2021-07-23 | 济南冶金化工设备有限公司 | Self-azeotropic negative pressure debenzolization process |
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