CN104403704B - Steam Heating washing oil negative pressure crude benzol distil process and equipment - Google Patents
Steam Heating washing oil negative pressure crude benzol distil process and equipment Download PDFInfo
- Publication number
- CN104403704B CN104403704B CN201410677117.3A CN201410677117A CN104403704B CN 104403704 B CN104403704 B CN 104403704B CN 201410677117 A CN201410677117 A CN 201410677117A CN 104403704 B CN104403704 B CN 104403704B
- Authority
- CN
- China
- Prior art keywords
- oil
- crude benzol
- tower
- benzene
- steam
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of Steam Heating washing oil negative pressure crude benzol distil process and equipment, utilize the on-condensible gas of the de-benzene series system of vavuum pump or sprayer pumps, make debenzolizing tower in negative-pressure operation state, in regenerator, steam and blow regeneration washing oil with steam, in debenzolizing tower, use the benzene class material in oil vapour or fresh superheated steam steaming purge oil that contains from regenerator. Compared with prior art, the invention has the beneficial effects as follows: 1) effectively contain washing oil slagging scorification, oil washing consumption is low; 2) utilize Steam Heating washing oil, homogeneous heating, washing oil polymerization amount is few; With the superheated steam washing oil of regenerating, ensure effective utilization of washing oil; 3) under certain vacuum degree, distill crude benzol, quantity of steam used reduces by 50% left and right, saves the energy, emission-free outer row, protection of the environment; 4) in debenzolizing tower, operating pressure is moderate, has ensured the condensation number of benzene in separator, has reduced a large amount of benzene class materials in the circulation of washing between benzene tower and debenzolizing tower, has reduced the treating capacity of equipment, has reduced operating cost.
Description
Technical field
The present invention relates to coking chemical product recovery technology field, relate in particular to the crude benzol distil process of Steam Heating washing oil negative pressureAnd equipment.
Background technology
At present, the crude benzol distil process of coking industry has the distillation of normal pressure crude benzol and two kinds of techniques of negative pressure crude benzol distillation.
Normal pressure crude benzol distil process is mainly the steam stripping distil process with diamond heating washing oil. This technique be 85～Under 185 DEG C of high temperature, operate, need to consume more primary energy (as steam, coke-stove gas etc.), crude benzol per ton or light benzeneNeed to consume approximately 1000～1500kg of steam, coal gas amount is 600～900Nm3/ t crude benzol, the about 100Kg/t crude benzol of oil washing consumption amount,Operating cost is high.
Compare with the distillation of normal pressure crude benzol, the distillation of negative pressure crude benzol is to distill in the debenzolizing tower of certain vacuum degree, obtains crude benzolOr the technological process of light benzene. This technique, according to different operating conditions, can reduce the primary energy energy resource consumption of different amounts.
The negative pressure crude benzol distil process of present stage is mainly that this technique is by debenzolizing tower without steaming process negative pressure crude benzol distil processEnd part washing oil circulating-heating in tube furnace, then deliver to the work of distilling crude benzol or light benzene in the debenzolizing tower of certain vacuum degreeSkill. This technique vacuum is high, and operating temperature is high, requires equipment corrosion resistance strong; Meanwhile, because vacuum is higher, vacuumAfter pump, will there is very most benzene to circulate washing in benzene tower and debenzolizing tower, need corresponding raising device processes ability, increase equipmentInvestment and operating cost; In addition, this technique need to increase a part of washing oil and heat in tube furnace, and heating after washing oil temperatureSpend highlyer, strengthened washing oil slagging scorification amount, washing oil loss strengthens; This technique is not because being used steam simultaneously, and residue oil is difficult for regenerationDegree is large, by circulating washing oil certain waste, increases operating cost.
In sum, the crude benzol distil process of present stage exists and lacks at aspects such as oil washing consumption, operating cost, the saving energyFall into, 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 oil washing consumption low, operationSimple and safe, emission-free outer row, operating cost be low, save the advantages such as the 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) absorbed the circulating washing oil of benzene class material coal gas and be pumped into poor oil-rich heat exchanger through rich oil from washing benzene tower, with de-benzeneAfter 170～185 DEG C of oil-poor heat exchange of heat of discharging at the bottom of tower, behind Steam Heating to 160～200 DEG C, enter debenzolizing tower ,-40～Under the gauge pressure of-70KPa, carry out stripping, distillation;
2) debenzolizing tower tower top is overflowed 55～70 DEG C of crude benzol or light benzene steam enter gas-liquid separator after condensate coolerCarry out gas-liquid separation, wherein incoagulable gas enters coal gas system through vavuum pump or injector, and liquid enters water-oil separatingDevice;
3) enter crude benzol or light benzene backflash by the isolated crude benzol of oil water separator or light benzene, wherein a part of crude benzol orPerson's light benzene is delivered to debenzolizing tower tower top as backflow with reflux pump, and all the other are as product introduction crude benzol or light benzene medial launder, then usesProduct pump is sent outside;
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 through oil-poor one sectionCooler, oil-poor two-step cooling device remove whole cold wash benzene device after being cooled to 27～29 DEG C.
Described circulating washing oil is drawn 1～1.5% and is sent in regenerator after the oil-poor pump of heat, and steam and blow regeneration with superheated steam,Regenerator top oil-containing gases enters debenzolizing tower, and at the bottom of tower, regeneration residue enters residue groove, regularly sends outside with pump.
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 steams.
Described debenzolizing tower side line is drawn naphtalene oil fraction, and the naphtalene oil fraction of drawing 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 of described debenzolizing tower entersMouthful be connected with washing oil heater, poor oil-rich heat exchanger successively, the steam (vapor) outlet at debenzolizing tower top successively with crude benzol or light benzene condensationCooler, vapour liquid separator, crude benzol or light benzene oil water 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 connect; The oil-poor outlet of heat of debenzolizing tower bottom successively with the oil-poor pump of heat,Poor oil-rich heat exchanger, oil-poor one section of cooler, oil-poor two-step cooling device connect; Outside debenzolizing tower is connected respectively with washing oil heaterPortion's jet chimney.
The oil-poor conveyance conduit of heat after the oil-poor pump of described heat connects regenerator in addition, establishes steam inlet and connect outside steaming on regeneratorSteam pipe road, the gas vent on regenerator 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 oil water separator of tower.
The outer oil water separator of described oil water separator or tower connects control separator in addition.
In described debenzolizing tower rectifying section, be provided with tower tray or filler, stripping section is packed tower structure.
Compared with prior art, the invention has the beneficial effects as follows:
1) in washing oil heater, operating temperature is low, has effectively contained the slagging scorification of washing oil, has reduced residue oil generation; Washing oilConsume and declined 50% by the about 100Kg/t crude benzol of traditional bed drain purge, save 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, washing oil polymerizationAmount is few; With the superheated steam washing oil of regenerating, ensure the gas oil ratio in regenerator, favorable regeneration effect in addition; Can ensure washing oilEffective utilization, reduced 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 50%Left and right, does not need coal gas, saves the energy, emission-free outer row, protection of the environment;
4) in debenzolizing tower, operating pressure is moderate, has ensured the condensation number of benzene in separator, has reduced a large amount of benzene class materials and has existedWash the circulation between benzene tower and debenzolizing tower, reduced accordingly the treating capacity of equipment, reduced operating cost.
Brief description of the drawings
Fig. 1 is process chart of the present invention.
In figure: 1. debenzolizing tower 2. regenerator 3. crude benzol or light benzene condensate cooler 4. gas-liquid separator 5. vavuum pumps orPerson's injector 6. crude benzol or light benzene oil water separator 7. control separator 8. crude benzol or light benzene backflash 9. crude benzol orHot oil-poor pump 13. lean and fat oils of light benzene reflux pump 10. crude benzol or light benzene medial launder 11. crude benzol or light benzene product pump 12. changeThe outer oil water separator of oil-poor two-step cooling device 16. washing oil heater 17. towers of the oil-poor one section of cooler 15. of hot device 14.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described further:
Seeing Fig. 1, is process chart of the present invention, and Steam Heating washing oil negative pressure crude benzol distil process of the present invention, comprisesFollowing steps:
1) absorbed the circulating washing oil of benzene class material coal gas and be pumped into poor oil-rich heat exchanger 13 through rich oil from washing benzene tower, withAfter 170～185 DEG C of oil-poor heat exchange of heat that discharge at 1 end of debenzolizing tower, behind Steam Heating to 160～200 DEG C, enter debenzolizing tower 1,Under the gauge pressure of-40～-70KPa, carry out stripping, distillation;
2) 55～70 DEG C of crude benzol that debenzolizing tower 1 tower top is overflowed or light benzene steam enter gas-liquid and divide after condensate cooler 3Carry out gas-liquid separation from device 4, wherein incoagulable gas enters coal gas system through vavuum pump or injector 5, and liquid entersOil water separator 6;
3) enter crude benzol or light benzene backflash 8 by the isolated crude benzol of oil water separator 6 or light benzene, wherein a part is thickBenzene or light benzene are delivered to debenzolizing tower 1 tower top as backflow with reflux pump 9, and all the other are as in the middle of product introduction crude benzol or light benzeneGroove 10, then send 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 warpOil-poor one section of cooler 14, oil-poor two-step cooling device 15 remove whole cold wash benzene device after being cooled to 27～29 DEG C.
Washing oil Steam Heating, oil product heating surface is even, there is no the hot heating surface of tube furnace, and washing oil is difficult for forming large molecule,Polymerization amount is few, the level of residue few (being that oil washing consumption is low) of generation, and simultaneously in order to keep circulating washing oil quality, circulating washing oil existsAfter the oil-poor pump 12 of heat, draw 1～1.5% and send in regenerator 2, steam and blow regeneration with superheated steam, regenerator 2 top gasBody enters debenzolizing tower 1, and at the bottom of tower, regeneration residue enters residue groove, regularly sends outside with pump.
The heating of described rich oil, debenzolizing tower 1 distill and circulating washing oil steam blow regeneration thermal source be 300～450 DEG C of superheated steams.
Described debenzolizing tower 1 side line is drawn naphtalene oil fraction, and to reduce the oil-poor naphthalene amount that contains, the naphtalene oil fraction of drawing enters residue groove,Regularly send outside with pump.
Of the present inventionly comprise debenzolizing tower 1 for realizing the equipment of Steam Heating washing oil negative pressure crude benzol distil process, described de-The rich oil entrance of benzene tower 1 is connected with washing oil heater 16, poor oil-rich heat exchanger 13 successively, and the steam at debenzolizing tower 1 top goes outMouth successively with crude benzol or light benzene condensate cooler 3, vapour liquid separator 4, crude benzol or light benzene oil water separator 6, crude benzol or lightBenzene 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 connect;The oil-poor outlet of heat of debenzolizing tower 1 bottom successively with the oil-poor pump 12 of heat, poor oil-rich heat exchanger 13, oil-poor one section of cooler 14,Oil-poor two-step cooling device 15 connects; Debenzolizing tower 1 is connected respectively external steam pipeline with washing oil heater 16.
The oil-poor conveyance conduit of heat after the oil-poor pump 12 of described heat connects regenerator 2 in addition, establishes steam inlet and connect on regenerator 2Connect external steam pipeline, the gas vent that regenerator 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 oil water separator 17 of tower, in order to draw tower top ponding, and stable behaviourMake process.
The outer oil water separator 17 of described oil water separator 6 or tower connects in addition controls separator 7.
In described debenzolizing tower 1 rectifying section, be provided with tower tray or filler, stripping section is packed tower structure.
Described debenzolizing tower 1, regenerator 2 and washing oil heater 16 are connected respectively external steam pipeline.
The present invention utilizes the on-condensible gas of the de-benzene series system of vavuum pump or injector 5 suction, make debenzolizing tower 1 in-40～The negative-pressure operation state of-70KPa (gauge pressure), steams and blows regeneration washing oil with steam regenerator 2 is interior, in debenzolizing tower 1, makesUse the benzene class material in oil vapour or fresh superheated steam steaming purge oil that contains from regenerator 2, de-benzene series system is separatedThe on-condensible gas such as benzene vapour deliver to coal gas system with vavuum pump or injector 5, to ensure the feature of environmental protection of technique and benzene class materialEffectively reclaim.
Claims (4)
1. Steam Heating washing oil negative pressure crude benzol distil process, is characterized in that, comprises the steps:
1) absorbed the circulating washing oil of benzene class material coal gas and be pumped into poor oil-rich heat exchanger through rich oil from washing benzene tower, with de-benzeneAfter 170～185 DEG C of oil-poor heat exchange of heat of discharging at the bottom of tower, behind Steam Heating to 160～200 DEG C, enter debenzolizing tower ,-40～Under the gauge pressure of-70KPa, carry out stripping, distillation;
2) debenzolizing tower tower top is overflowed 55～70 DEG C of crude benzol or light benzene steam enter gas-liquid separator after condensate coolerCarry out gas-liquid separation, wherein incoagulable gas enters coal gas system through vavuum pump or injector, and liquid enters water-oil separatingDevice;
3) enter crude benzol or light benzene backflash by the isolated crude benzol of oil water separator or light benzene, wherein a part of crude benzol orPerson's light benzene is delivered to debenzolizing tower tower top as backflow with reflux pump, and all the other are as product introduction crude benzol or light benzene medial launder, then usesProduct pump is sent outside;
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 through oil-poor one sectionCooler, oil-poor two-step cooling device remove whole cold wash benzene device after being cooled to 27～29 DEG C.
2. Steam Heating washing oil negative pressure crude benzol distil process according to claim 1, is characterized in that described circulationWashing oil is drawn 1～1.5% and is sent in regenerator after the oil-poor pump of heat, steams and blows regeneration, regenerator top oil-containing with superheated steamGas enters debenzolizing tower, and at the bottom of tower, regeneration residue enters residue groove, regularly sends outside with pump.
3. Steam Heating washing oil negative pressure crude benzol distil process according to claim 1, is characterized in that described rich oilHeating, debenzolizing tower distillation and circulating washing oil steam blow regeneration thermal source be 300～450 DEG C of superheated steams.
4. Steam Heating washing oil negative pressure crude benzol distil process according to claim 1, is characterized in that described de-benzeneTower side line is drawn naphtalene oil fraction, and the naphtalene oil fraction of drawing enters residue groove, regularly sends outside with pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410677117.3A CN104403704B (en) | 2014-11-21 | 2014-11-21 | Steam Heating washing oil negative pressure crude benzol distil process and equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410677117.3A CN104403704B (en) | 2014-11-21 | 2014-11-21 | Steam Heating washing oil negative pressure crude benzol distil process and equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104403704A CN104403704A (en) | 2015-03-11 |
| CN104403704B true CN104403704B (en) | 2016-05-11 |
Family
ID=52641376
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410677117.3A Active CN104403704B (en) | 2014-11-21 | 2014-11-21 | Steam Heating washing oil negative pressure crude benzol distil process and equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104403704B (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104962323B (en) * | 2015-06-26 | 2017-10-27 | 山东钢铁股份有限公司 | A kind of renovation process of negative pressure benzene removal circulating washing oil |
| CN105062575B (en) * | 2015-08-03 | 2018-01-16 | 中冶焦耐工程技术有限公司 | Control the technique and device of incoagulable gas continuous-stable discharge in benzene recovery system |
| 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 |
| 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 |
| 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 |
| CN112933633B (en) * | 2021-04-12 | 2023-03-24 | 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 |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102408298B (en) * | 2011-09-21 | 2014-03-19 | 宝钢工程技术集团有限公司 | Method of distilling crude benzene by decompression method and device thereof |
| CN204265717U (en) * | 2014-11-21 | 2015-04-15 | 中冶焦耐工程技术有限公司 | Steam heating washing oil negative pressure crude benzol distillation plant |
-
2014
- 2014-11-21 CN CN201410677117.3A patent/CN104403704B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN104403704A (en) | 2015-03-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104403704B (en) | Steam Heating washing oil negative pressure crude benzol distil process and equipment | |
| CN102796537B (en) | System and method for recovering superheated steam of waste heat of raw gas of combined coke oven | |
| CN102408298B (en) | Method of distilling crude benzene by decompression method and device thereof | |
| CN101476825B (en) | Phase-change heat-exchange type secondary steam heat recovery utilization method, apparatus and use thereof | |
| CN103555377B (en) | A kind of de-benzene method of decompression | |
| CN108096999B (en) | Reboiler method negative pressure crude benzene distillation process | |
| CN102241418A (en) | Negative pressure distillation equipment and method for residual ammonia water | |
| CN204265717U (en) | Steam heating washing oil negative pressure crude benzol distillation plant | |
| CN104848284A (en) | Steam condensation water heat recovery method and device | |
| CN102602960B (en) | Method for stilling ammonia by aid of waste heat of flue gas of coke oven and equipment | |
| CN101993736B (en) | Method and device for regenerating circular wash oil during rich oil debenzolization of gas purification | |
| CN104312638B (en) | Thermal coupling negative pressure benzene removal, regeneration integrated apparatus | |
| CN107890684B (en) | Reboiler method negative pressure crude benzol distillation system | |
| CN103848476B (en) | Electrically trapped tar oil waste water multi-phase separation technique | |
| CN204162673U (en) | Thermal coupling negative pressure benzene removal, regeneration integrated apparatus | |
| CN210656809U (en) | Tar negative pressure dewatering system | |
| CN104789273A (en) | System for recycling coke oven raw-gas benzene substances by using raw-gas waste heat | |
| CN204026651U (en) | A kind of closed condensate water recovery device | |
| CN203904017U (en) | High-efficiency ammonia distillation system for surplus ammonia water | |
| CN106277677A (en) | A kind of mud combination treatment method and device | |
| CN210945430U (en) | Recovery unit of crude benzol | |
| CN203768322U (en) | Negative-pressure distilled benzene circulating washing oil regeneration device | |
| CN207734627U (en) | A kind of reboiler method negative pressure crude benzol Distallation systm | |
| CN105567309A (en) | Waste mineral oil circulating flash-evaporation catalytic cracking recovery plant | |
| CN217323988U (en) | Negative pressure debenzolization device for circulating wash oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
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 |