CN104403704A - Negative-pressure crude benzene distillation process and equipment heating washing oil by steam - Google Patents
Negative-pressure crude benzene distillation process and equipment heating washing oil by steam Download PDFInfo
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- CN104403704A CN104403704A CN201410677117.3A CN201410677117A CN104403704A CN 104403704 A CN104403704 A CN 104403704A CN 201410677117 A CN201410677117 A CN 201410677117A CN 104403704 A CN104403704 A CN 104403704A
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- oil
- tower
- crude benzol
- poor
- washing oil
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
- C10K1/18—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids hydrocarbon oils
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention relates to a negative-pressure crude benzene distillation process and equipment heating washing oil by steam. Non-condensable gas of a debenzolization system is sucked by a vacuum pump or an ejector, so a debenzolization tower is in a negative-pressure operation state; washing oil is steamed, blown and regenerated by steam in a regenerator, and benzene homologs and derivates in the washing oil are steamed and blown by steam containing oil or fresh overheated steam obtained from the regenerator in the debenzolization tower. Compared with the prior art, the negative-pressure crude benzene distillation process and equipment have the benefits that (1) slagging of the washing oil is effectively prevented and the consumption of the washing oil is low; (2) the washing oil is heated uniformly by the steam, the amount of polymerized washing oil is small, the washing oil is regenerated by the overheated steam and accordingly the effective use of the washing oil is guaranteed; (3) crude benzene is distilled in a certain vacuum degree, the amount of steam used in the process is reduced by about 50%, the energy is saved, exhaust of tail gas is avoided and environmental protection is achieved; (4) the operation pressure in the debenzolization tower is moderate, the amount of condensed benzene in a separator is reduced, circulation of a large quantity of the benzene homologs and derivates between a crude benzene scrubber and the debenzolization tower is reduced, the treatment load of the equipment is reduced and the operation cost is reduced.
Description
Technical field
The present invention relates to coking chemical Product recycling technical field, particularly relate to crude benzol distil process and the equipment of steam heating washing oil negative pressure.
Background technology
At present, the crude benzol distil process of coking industry has the distillation of normal pressure crude benzol and negative pressure crude benzol to distill two kinds of techniques.
Normal pressure crude benzol distil process mainly uses the steam stripped distil process of diamond heating washing oil.This technique operates under 85 ~ 185 DEG C of high temperature, needs to consume more primary energy source (as steam, coke-oven gas etc.), and crude benzol per ton or light benzene need consume steam about 1000 ~ 1500kg, and coal gas amount is 600 ~ 900Nm
3/ t crude benzol, oil washing consumption amount is about 100Kg/t crude benzol, and process cost is high.
Compared with distilling with normal pressure crude benzol, the distillation of negative pressure crude benzol is distilled in the debenzolizing tower of certain vacuum degree, obtains the technical process of crude benzol or light benzene.This technique, according to different operational conditions, can reduce the primary energy source energy consumption of different amount.
The negative pressure crude benzol distil process of present stage is mainly without steaming process negative pressure crude benzol distil process, and this technique is by part washing oil at the bottom of debenzolizing tower in the heating of tube furnace internal recycle, then delivers to the debenzolizing tower interior distillation crude benzol of certain vacuum degree or the technique of light benzene.This technique vacuum tightness is high, and service temperature is high, requires that equipment corrosion resistance is strong; Meanwhile, because vacuum tightness is higher, very most benzene after vacuum pump, will be had to wash benzene tower and debenzolizing tower internal recycle, and need corresponding raising device processes ability, add facility investment and running cost; In addition, this technique needs to increase a part of washing oil and heats in tube furnace, and heating after washing oil temperature higher, increase washing oil slagging scorification amount, washing oil loss strengthen; This technique is not because using steam simultaneously, and residual oil regeneration difficulty is large, by circulating washing oil certain for waste, increases running cost.
In sum, crude benzol distil process existing defects in oil washing consumption, running cost, save energy etc. of present stage, anxious to be resolved.
Summary of the invention
The invention provides a kind of crude benzol distil process and equipment of steam heating washing oil negative pressure, have that low, simple to operate safe, the emission-free outer row of oil washing consumption, running cost are low, the advantage such as save energy and environmental protection.
In order to achieve the above object, the present invention realizes by the following technical solutions:
Steam heating washing oil negative pressure crude benzol distil process, comprises the steps:
1) poor oil-rich heat exchanger is pumped into from the circulating washing oil washing benzene tower and absorb benzene class material coal gas through rich oil, after 170 ~ 185 DEG C of oil-poor heat exchange of heat of discharging at the bottom of debenzolizing tower, after steam heating is to 160 ~ 200 DEG C, enters debenzolizing tower, under the gauge pressure of-40 ~-70KPa, carries out stripping, distillation;
2) 55 ~ 70 DEG C of crude benzol of debenzolizing tower tower top effusion or light benzene steam enter gas-liquid separator and carry out gas-liquid separation after condensate cooler, and wherein non-condensable gases enters coal gas system through vacuum pump or injector, and liquid enters water-and-oil separator;
3) crude benzol or light benzene backflash is entered by the isolated crude benzol of water-and-oil separator or light benzene, wherein a part of crude benzol or light benzene reflux pump deliver to debenzolizing tower tower top as backflow, all the other as product introduction crude benzol or light benzene medial launder, then are sent outside with product pump;
4) the hot oil-poor pump of the oil-poor use of heat of discharging at the bottom of debenzolizing tower is extracted out, after poor oil-rich heat exchanger heat exchange, then removes whole cold wash benzene device after being cooled to 27 ~ 29 DEG C through oil-poor one-step cooling device, oil-poor two-step cooling device.
Described circulating washing oil is drawn 1 ~ 1.5% and is sent in revivifier after the oil-poor pump of heat, and carry out steaming with superheated vapour and blow regeneration, revivifier top oil-containing gases enters debenzolizing tower, regenerates residue and enters residue groove, regularly send outside with pump at the bottom of tower.
The heating of described rich oil, debenzolizing tower distillation and circulating washing oil steam blow regeneration thermal source be 300 ~ 450 DEG C of superheated vapours.
Naphtalene oil fraction drawn by described debenzolizing tower side line, and the naphtalene oil fraction of extraction enters residue groove, regularly sends outside with pump.
For realizing the equipment of steam heating washing oil negative pressure crude benzol distil process, comprise debenzolizing tower, the rich oil entrance of described debenzolizing tower is connected with washing oil well heater, poor oil-rich heat exchanger successively, and the vapour outlet at debenzolizing tower top is connected with crude benzol or light benzene condensate cooler, vapour liquid separator, crude benzol or light benzene water-and-oil separator, crude benzol or light benzene backflash, crude benzol or light benzene reflux pump, crude benzol or light benzene medial launder, crude benzol or light benzene product pump successively; The oil-poor outlet of heat bottom debenzolizing tower successively pump oil-poor with heat, poor oil-rich heat exchanger, oil-poor one-step cooling device, oil-poor two-step cooling device is connected; Debenzolizing tower is connected external steam pipeline respectively with washing oil well heater.
The oil-poor transport pipe of heat after the oil-poor pump of described heat connects revivifier in addition, revivifier is established steam-in connect external steam pipeline, and the pneumatic outlet on revivifier top connects the oil-containing vapour inlet of debenzolizing tower bottom.
The top of described debenzolizing tower is provided with disconnected tower tray and the outer water-and-oil separator of tower.
Described water-and-oil separator or the outer other connection control separator of water-and-oil separator of tower.
Be provided with tower tray or filler in described debenzolizing tower rectifying section, stripping section is packing tower structure.
Compared with prior art, the invention has the beneficial effects as follows:
1) in washing oil well heater, service temperature is low, has effectively contained the slagging scorification of washing oil, has reduced residual oil generation; Oil washing consumption is about 100Kg/t crude benzol by traditional bed drain purge and have dropped 50%, saves the cost of primary material;
2) compared with other negative pressure crude benzol distil process, the present invention utilizes steam heating washing oil, homogeneous heating, and washing oil polymerization amount is few; Regenerate washing oil with superheated vapour in addition, ensure that the gas oil ratio in revivifier, favorable regeneration effect; Effective utilization of washing oil can be ensured, decrease the waste of washing oil;
3) compared with malleation crude benzol distil process, the present invention distills crude benzol under certain vacuum degree, and quantity of steam used reduces about 50%, does not need coal gas, save energy, emission-free outer row, protection of the environment;
4) in debenzolizing tower, working pressure is moderate, ensure that the condensation number of benzene in separator, decreases a large amount of benzene class materials and is washing the circulation between benzene tower and debenzolizing tower, consequently reduce the treatment capacity of equipment, reduce running cost.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
In figure: 1. debenzolizing tower 2. revivifier 3. crude benzol or light benzene condensate cooler 4. gas-liquid separator 5. vacuum pump or injector 6. crude benzol or light benzene water-and-oil separator 7. control separator 8. crude benzol or light benzene backflash 9. crude benzol or light benzene reflux pump 10. crude benzol or light benzene medial launder 11. crude benzol or the outer water-and-oil separator of the light benzene product pump 12. oil-poor one-step cooling device 15. of hot oil-poor pump 13. poor oil-rich heat exchanger 14. oil-poor two-step cooling device 16. washing oil well heater 17. tower
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described further:
Seeing Fig. 1, is process flow sheet of the present invention, and steam heating washing oil negative pressure crude benzol distil process of the present invention, comprises the steps:
1) poor oil-rich heat exchanger 13 is pumped into from the circulating washing oil washing benzene tower and absorb benzene class material coal gas through rich oil, after 170 ~ 185 DEG C of oil-poor heat exchange of heat of discharging with debenzolizing tower 1 end, after steam heating is to 160 ~ 200 DEG C, enters debenzolizing tower 1, under the gauge pressure of-40 ~-70KPa, carries out stripping, distillation;
2) 55 ~ 70 DEG C of crude benzol of debenzolizing tower 1 tower top effusion or light benzene steam enter gas-liquid separator 4 and carry out gas-liquid separation after condensate cooler 3, and wherein non-condensable gases enters coal gas system through vacuum pump or injector 5, and liquid enters water-and-oil separator 6;
3) crude benzol or light benzene backflash 8 is entered by the isolated crude benzol of water-and-oil separator 6 or light benzene, wherein a part of crude benzol or light benzene reflux pump 9 deliver to debenzolizing tower 1 tower top as backflow, all the other as product introduction crude benzol or light benzene medial launder 10, then are sent outside with product pump 11;
4) the hot oil-poor pump 12 of the oil-poor use of heat of debenzolizing tower 1 end discharge is extracted out, after poor oil-rich heat exchanger 13 heat exchange, then removes whole cold wash benzene device after being cooled to 27 ~ 29 DEG C through oil-poor one-step cooling device 14, oil-poor two-step cooling device 15.
Washing oil steam heating, oil product heating surface is even, and do not have the hot face that tube furnace is hot, washing oil not easily forms macromole, polymerization amount is few, the level of residue few (namely oil washing consumption is low) produced, simultaneously in order to keep circulating washing oil quality, circulating washing oil is drawn 1 ~ 1.5% and is sent in revivifier 2 after the oil-poor pump 12 of heat, carry out steaming with superheated vapour and blow regeneration, revivifier 2 top gas body enters debenzolizing tower 1, regenerates residue and enters residue groove, regularly send outside with pump at the bottom of tower.
The heating of described rich oil, debenzolizing tower 1 are distilled and circulating washing oil steam blow regeneration thermal source be 300 ~ 450 DEG C of superheated vapours.
Naphtalene oil fraction drawn by described debenzolizing tower 1 side line, and oil-poor containing naphthalene amount to reduce, the naphtalene oil fraction of extraction enters residue groove, regularly sends outside with pump.
Equipment for realizing steam heating washing oil negative pressure crude benzol distil process of the present invention, comprise debenzolizing tower 1, the rich oil entrance of described debenzolizing tower 1 is connected with washing oil well heater 16, poor oil-rich heat exchanger 13 successively, and the vapour outlet at debenzolizing tower 1 top is connected with crude benzol or light benzene condensate cooler 3, vapour liquid separator 4, crude benzol or light benzene water-and-oil separator 6, crude benzol or light benzene backflash 8, crude benzol or light benzene reflux pump 9, crude benzol or light benzene medial launder 10, crude benzol or light benzene product pump 11 successively; The oil-poor outlet of heat bottom debenzolizing tower 1 successively pump 12 oil-poor with heat, poor oil-rich heat exchanger 13, oil-poor one-step cooling device 14, oil-poor two-step cooling device 15 is connected; Debenzolizing tower 1 is connected external steam pipeline respectively with washing oil well heater 16.
The oil-poor transport pipe of heat after the oil-poor pump of described heat 12 connects revivifier 2 in addition, and revivifier 2 is established steam-in connect external steam pipeline, the pneumatic outlet that revivifier 2 pushes up connects the oil-containing vapour inlet of debenzolizing tower 1 bottom.
The top of described debenzolizing tower 1 is provided with disconnected tower tray and the outer water-and-oil separator 17 of tower, in order to draw tower top ponding, and stable operation process.
Described water-and-oil separator 6 or the outer water-and-oil separator 17 of tower connection control separator 7 in addition.
Be provided with tower tray or filler in described debenzolizing tower 1 rectifying section, stripping section is packing tower structure.
Described debenzolizing tower 1, revivifier 2 are connected external steam pipeline respectively with washing oil well heater 16.
The present invention utilizes vacuum pump or injector 5 to aspirate the noncondensable gas of de-benzene series system, debenzolizing tower 1 is made to be in the negative-pressure operation state of-40 ~-70KPa (gauge pressure), in revivifier 2, carry out steaming with steam blow regeneration washing oil, the benzene class material steamed containing oil vapour or fresh superheated vapour in purge oil from revivifier 2 is used in debenzolizing tower 1, the unite noncondensable gas vacuum pumps such as the benzene vapour separated or injector 5 of de-benzene series delivers to coal gas system, with the efficient recovery of the feature of environmental protection and benzene class material that ensure technique.
Claims (10)
1. steam heating washing oil negative pressure crude benzol distil process, is characterized in that, comprise the steps:
1) poor oil-rich heat exchanger is pumped into from the circulating washing oil washing benzene tower and absorb benzene class material coal gas through rich oil, after 170 ~ 185 DEG C of oil-poor heat exchange of heat of discharging at the bottom of debenzolizing tower, after steam heating is to 160 ~ 200 DEG C, enters debenzolizing tower, under the gauge pressure of-40 ~-70KPa, carries out stripping, distillation;
2) 55 ~ 70 DEG C of crude benzol of debenzolizing tower tower top effusion or light benzene steam enter gas-liquid separator and carry out gas-liquid separation after condensate cooler, and wherein non-condensable gases enters coal gas system through vacuum pump or injector, and liquid enters water-and-oil separator;
3) crude benzol or light benzene backflash is entered by the isolated crude benzol of water-and-oil separator or light benzene, wherein a part of crude benzol or light benzene reflux pump deliver to debenzolizing tower tower top as backflow, all the other as product introduction crude benzol or light benzene medial launder, then are sent outside with product pump;
4) the hot oil-poor pump of the oil-poor use of heat of discharging at the bottom of debenzolizing tower is extracted out, after poor oil-rich heat exchanger heat exchange, then removes whole cold wash benzene device after being cooled to 27 ~ 29 DEG C through oil-poor one-step cooling device, oil-poor two-step cooling device.
2. steam heating washing oil negative pressure crude benzol distil process according to claim 1, it is characterized in that, described circulating washing oil is drawn 1 ~ 1.5% and is sent in revivifier after the oil-poor pump of heat, carry out steaming with superheated vapour and blow regeneration, revivifier top oil-containing gases enters debenzolizing tower, regenerate residue at the bottom of tower and enter residue groove, regularly send outside with pump.
3. steam heating washing oil negative pressure crude benzol distil process according to claim 1, is characterized in that, the heating of described rich oil, debenzolizing tower distillation and circulating washing oil steam blow regeneration thermal source be 300 ~ 450 DEG C of superheated vapours.
4. steam heating washing oil negative pressure crude benzol distil process according to claim 1, is characterized in that, naphtalene oil fraction drawn by described debenzolizing tower side line, and the naphtalene oil fraction of extraction enters residue groove, regularly sends outside with pump.
5. for realizing the equipment of steam heating washing oil negative pressure crude benzol distil process according to claim 1, it is characterized in that, comprise debenzolizing tower, the rich oil entrance of described debenzolizing tower is connected with washing oil well heater, poor oil-rich heat exchanger successively, and the vapour outlet at debenzolizing tower top is connected with crude benzol or light benzene condensate cooler, vapour liquid separator, crude benzol or light benzene water-and-oil separator, crude benzol or light benzene backflash, crude benzol or light benzene reflux pump, crude benzol or light benzene medial launder, crude benzol or light benzene product pump successively; The oil-poor outlet of heat bottom debenzolizing tower successively pump oil-poor with heat, poor oil-rich heat exchanger, oil-poor one-step cooling device, oil-poor two-step cooling device is connected; Debenzolizing tower is connected external steam pipeline respectively with washing oil well heater.
6. steam heating washing oil negative pressure crude benzol distillation plant according to claim 5, it is characterized in that, the oil-poor transport pipe of heat after the oil-poor pump of described heat connects revivifier in addition, revivifier is established steam-in connect external steam pipeline, the pneumatic outlet on revivifier top connects the oil-containing vapour inlet of debenzolizing tower bottom.
7. steam heating washing oil negative pressure crude benzol distillation plant according to claim 5, is characterized in that, the top of described debenzolizing tower is provided with disconnected tower tray and the outer water-and-oil separator of tower.
8. the steam heating washing oil negative pressure crude benzol distillation plant according to claim 5 or 7, is characterized in that, described water-and-oil separator or the outer other connection control separator of water-and-oil separator of tower.
9. steam heating washing oil negative pressure crude benzol distillation plant according to claim 5, it is characterized in that, be provided with tower tray or filler in described debenzolizing tower rectifying section, stripping section is packing tower structure.
10. steam heating washing oil negative pressure crude benzol distillation plant according to claim 5, it is characterized in that, described debenzolizing tower, revivifier are connected external steam pipeline respectively with washing oil well heater.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410677117.3A CN104403704B (en) | 2014-11-21 | 2014-11-21 | Steam Heating washing oil negative pressure crude benzol distil process and equipment |
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| CN201410677117.3A CN104403704B (en) | 2014-11-21 | 2014-11-21 | Steam Heating washing oil negative pressure crude benzol distil process and equipment |
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| CN104403704B CN104403704B (en) | 2016-05-11 |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104962323A (en) * | 2015-06-26 | 2015-10-07 | 山东钢铁股份有限公司 | Regeneration method of negative pressure debenzolization circulation washing oil |
| CN105062575A (en) * | 2015-08-03 | 2015-11-18 | 中冶焦耐工程技术有限公司 | Process and apparatus for controlling continuous and stable discharge of non-condensable gas in benzene recovery system |
| CN105293606A (en) * | 2015-10-23 | 2016-02-03 | 鲁西化工集团股份有限公司 | Recovery system and recovery method of oily waste liquor in cyclohexanol production process |
| CN107628923A (en) * | 2017-09-29 | 2018-01-26 | 王书虎 | A kind of negative pressure benzene removal system and method for rich oil half |
| 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 |
| CN108380005A (en) * | 2018-04-17 | 2018-08-10 | 沂州科技有限公司 | A kind of de- benzene device of low energy consumption local decompression and its de- benzene method |
| 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 |
| CN111849565A (en) * | 2019-09-20 | 2020-10-30 | 萍乡市华星环保工程技术有限公司 | Novel debenzolization tower for coking chemical products |
| CN112280599A (en) * | 2020-11-19 | 2021-01-29 | 中冶焦耐(大连)工程技术有限公司 | Vertical multi-section heating and distillation integrated washing oil regeneration equipment |
| CN112933633A (en) * | 2021-04-12 | 2021-06-11 | 孝义市金精化工有限公司 | Negative-pressure continuous distillation and separation device for coal tar washing oil and coal tar washing oil separation and refining method |
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104962323A (en) * | 2015-06-26 | 2015-10-07 | 山东钢铁股份有限公司 | Regeneration method of negative pressure debenzolization circulation washing oil |
| CN105062575A (en) * | 2015-08-03 | 2015-11-18 | 中冶焦耐工程技术有限公司 | Process and apparatus for controlling continuous and stable discharge of non-condensable gas in benzene recovery system |
| CN105293606A (en) * | 2015-10-23 | 2016-02-03 | 鲁西化工集团股份有限公司 | Recovery system and recovery method of oily waste liquor in cyclohexanol production process |
| CN105293606B (en) * | 2015-10-23 | 2017-08-25 | 鲁西化工集团股份有限公司 | Oily waste liquor recovery system and recovery method during a kind of cyclohexanol production |
| CN107628923A (en) * | 2017-09-29 | 2018-01-26 | 王书虎 | A kind of negative pressure benzene removal system and method for rich oil half |
| 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 |
| 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 |
| CN108380005A (en) * | 2018-04-17 | 2018-08-10 | 沂州科技有限公司 | A kind of de- benzene device of low energy consumption local decompression and its de- benzene method |
| 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 |
| CN111849565A (en) * | 2019-09-20 | 2020-10-30 | 萍乡市华星环保工程技术有限公司 | Novel debenzolization tower for coking chemical products |
| 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 |
| CN112280599A (en) * | 2020-11-19 | 2021-01-29 | 中冶焦耐(大连)工程技术有限公司 | Vertical multi-section heating and distillation integrated washing oil regeneration equipment |
| CN112933633A (en) * | 2021-04-12 | 2021-06-11 | 孝义市金精化工有限公司 | Negative-pressure continuous distillation and separation device for coal tar washing oil and coal tar washing oil separation and refining method |
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Effective date of registration: 20180802 Address after: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee after: ACRE Coking And Refractory (Dalian) Engineering Consulting Corp., MCC Address before: 116085 128 high energy street, Qixian Ling high tech Industrial Park, Dalian, Liaoning Patentee before: ACRE Coking and Refractory Engineering Consulting Corporation, MCC |