CN106008457A - Solvent regenerating process and device for crude benzene refining process - Google Patents
Solvent regenerating process and device for crude benzene refining process Download PDFInfo
- Publication number
- CN106008457A CN106008457A CN201610585634.7A CN201610585634A CN106008457A CN 106008457 A CN106008457 A CN 106008457A CN 201610585634 A CN201610585634 A CN 201610585634A CN 106008457 A CN106008457 A CN 106008457A
- Authority
- CN
- China
- Prior art keywords
- solvent
- blender
- water
- aromatics
- extraction
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D333/00—Heterocyclic compounds containing five-membered rings having one sulfur atom as the only ring hetero atom
- C07D333/02—Heterocyclic compounds containing five-membered rings having one sulfur atom as the only ring hetero atom not condensed with other rings
- C07D333/46—Heterocyclic compounds containing five-membered rings having one sulfur atom as the only ring hetero atom not condensed with other rings substituted on the ring sulfur atom
- C07D333/48—Heterocyclic compounds containing five-membered rings having one sulfur atom as the only ring hetero atom not condensed with other rings substituted on the ring sulfur atom by oxygen atoms
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a solvent regenerating process and device for crude benzene refining process. When heavy hydrocarbon component content included in a circulating lean solvent is >3% by weight, lean solvent extracted from the bottom of a solvent recycling column is not directly fed into a solvent regenerating column any longer but purified first; the lean solvent is mixed successively with non-aromatic hydrocarbons and water, non-aromatic hydrocarbon and heavy hydrocarbon components are isolated via a two-stage isolating tank, and a water and solvent mixture enters a water stripping column to further isolate non-aromatic hydrocarbons and water; the purified lean solvent is returned to the solvent recycling column through the solvent regenerating column. Solvent purifying process is added before conventional solvent regenerating process, the lean solvent from the solvent recycling column to the solvent regenerating column is purified first when the heavy hydrocarbon component content in the lean solvent regenerated by steam stripping is >3% by weight, and heavy hydrocarbon components in the solvent are removed effectively; the process is simple to perform, utilization rate of the solvent is greatly increased, and economic benefit is improved; heat load and wastewater are not additionally increased, investment is low, and the effect is good.
Description
Technical field
The present invention relates to hydrofining coking crude benzene production technical field, particularly relate to solvent reclamation during a kind of crude benzene refining
Technique and device.
Background technology
Alkane that the purpose of crude benzene refining seeks to remove in crude benzol, alkene, sulfur-bearing compounds and miscellaneous containing nitrogen compound etc.
Matter, then through products such as rectification isolated purified petroleum benzin, pure toluene, dimethylbenzene.
The brief flow process of extractive distillation technique with sulfolane as solvent is as follows:
Hydrogenated oil after stabilizer is directly entered as extraction feed in the middle part of extraction distillation column, lean from come at the bottom of solvent recovery tower
Solvent enters the top of extraction distillation column and completes to extract with non-aromatics steam generation phase mass transfer with the aromatic hydrocarbons of rising in tower
Journey, aromatic hydrocarbons is dissolved in a solvent, falls at the bottom of tower；The non-aromatics such as alkane, cycloalkane do not dissolve in solvent, non-aromatics steam from
Extraction distillation column top is sent after supercooling.The rich solvent of extraction at the bottom of tower delivers to solvent recovery tower rectification under vacuum, after extracting
Hydrocarbon mixture separate from rich solvent.In order to improve separating effect, by solvent recovery tower injects water vapour stripping, have
Effect ground reduces energy consumption.The lean solvent 99% of extraction at the bottom of solvent recovery tower is circulated back to extractive distillation column top after cooling, and 1% send
To solvent regeneration tower steam stripping, discharging high boiling polymerizate under vacuum conditions, the solvent after regeneration returns to solvent and returns
Receive in tower.The benzene distillation part that the hydrocarbon mixture of solvent recovery tower top enters after cooling continues to separate, and the separation water collected is at water
Stripper refills in system after stripping, recycles.
In actual production running, due to crude benzol raw material composition complexity, and composition fluctuation ratio is relatively big, C8 and above
Heavy hydrocarbon component is built up the most in a solvent.Under normal production conditions, after sulfolane solvent recycles 2 months, purity will
Dropping to less than 97%, the regeneration lean solvent obtained only with steam stripping regeneration method can not meet production requirement.
Summary of the invention
The invention provides solvent regeneration process and device during a kind of crude benzene refining, increase before Conventional solvents regeneration technology
Solvent purifying technique, as heavy hydrocarbon component content ＞ 3wt% in the lean solvent that steam stripping regenerates, solvent recovery tower is gone to molten
The first purified process of the lean solvent of agent regenerator, effectively removes the heavy hydrocarbon component in solvent；It is simple to operate, is greatly improved
Solvent utilization rate, increases economic benefit；And the most additionally increase thermic load and wastewater flow rate, small investment, effective；The present invention
Provide the device for realizing this technique simultaneously.
In order to achieve the above object, the present invention realizes by the following technical solutions:
Solvent regeneration process during a kind of crude benzene refining, in normal productive process, the hydrogenated oil after stabilizer is directly entered
As extraction feed in the middle part of extraction distillation column, enter from the lean solvent come at the bottom of solvent recovery tower in top and the tower of extraction distillation column
The aromatic hydrocarbons risen and non-aromatics steam generation phase mass transfer complete extraction process, and non-aromatics is from rich solvent at the bottom of overhead extraction, tower
Enter solvent recovery tower rectification under vacuum, and inject water vapour stripping；Extraction lean solvent at the bottom of solvent recovery tower, therein 99%
Returning to extraction distillation column top after cooling recycle, 1% additionally is delivered to solvent regeneration tower and is regenerated through steam stripping；
Also comprise the steps:
1) the circulation lean solvent entering extraction distillation column is carried out regular pick test, as contained heavy hydrocarbon component content ＞ 3wt%
Time, the lean solvent of extraction at the bottom of solvent recovery tower is no longer sent directly in solvent regeneration tower, but first purified process；
2) 1%～2% feeding blender one in the circulation lean solvent of extraction distillation column will be entered, and from extractive distillation column overhead
The non-aromatics Product mix of extraction, mixed mixture one sends into blender two；It is sequentially provided with two-stage after blender two to separate
Groove, the water drawn from the second-order separation trench bottom and solvent mixture, also into blender two, are mixed to get mixed with mixture one
Compound two；
3) mixture two enters flash trapping stage groove, separated after, water and solvent are miscible and be deposited on flash trapping stage groove bottom shape
Becoming heavy phase, non-aromatics is dissolved heavy hydrocarbon component and is formed light phase on flash trapping stage groove top；Gently, heavy phase layering after, flash trapping stage groove
Top non-aromatics and the water in heavy hydrocarbon component and solvent recovery tower and benzene distillation tower backflash water shoes are the most mixed in blender three
Close, obtain mixture three；The water of flash trapping stage groove bottom and solvent mixture enter water stripper；
4) mixture three enters the second-order separation groove, separated after, water and solvent are miscible and be deposited on the second-order separation groove bottom shape
Becoming heavy phase, non-aromatics is dissolved heavy hydrocarbon component and is formed light phase on the second-order separation groove top；Gently, heavy phase layering after, the second-order separation groove
Top non-aromatics and heavy hydrocarbon component are delivered to collect in non-aromatics heavy hydrocarbon component collecting tank；The water of the second-order separation groove bottom and solvent mix
Compound enters in blender two；
5) in water stripper, after stripping, non-aromatics product is isolated from the water in flash trapping stage groove and solvent mixture
And water, and obtain purifying lean solvent；Non-aromatics product sends into extractive distillation column overhead, purifies lean solvent after solvent regeneration tower
Enter solvent recovery tower；
6) as contained heavy hydrocarbon component content≤3wt% in inspection to circulation lean solvent, the lean solvent of extraction at the bottom of solvent recovery tower
The most purified process, is sent directly in solvent regeneration tower.
In described blender one, the mixed volume of lean solvent and non-aromatics product is than for 1:2～3；In blender two, mixing
Thing one mixes with arbitrary proportion with water and solvent mixture；In blender three, the water in non-aromatics, heavy hydrocarbon component and water shoes with
Arbitrary proportion mixes.
The described mixture two disengaging time in flash trapping stage groove, the mixture three disengaging time in the second-order separation groove are the biggest
In 4 hours.
During realizing a kind of crude benzene refining, the solvent reclamation device of solvent regeneration process, is sequentially connected with including by pipeline
Blender one, blender two, flash trapping stage groove, blender three, the second-order separation groove and non-aromatics heavy hydrocarbon component collecting tank；
Input channel one before blender one connects the non-aromatics product extraction mouth of extractive distillation tower top；Input channel before blender one
The two lean solvent outlets connecting solvent recovery tower；Input channel three before blender two connects the outlet of blender one, blender
Input channel four before two connects the second-order separation trench bottom extraction mouth；The output channel of blender two connects entering of flash trapping stage groove
Mouthful；Input channel five before blender three connects the top extraction mouth of flash trapping stage groove, and the input channel six before blender three is even
Connect solvent recovery tower and benzene distillation tower backflash water shoes, the entrance of the output channel connection the second-order separation groove of blender three, two grades
The top extraction mouth of separating tank connects non-aromatics heavy hydrocarbon component collecting tank；Flash trapping stage trench bottom extraction mouth connects water stripper and enters
Mouthful.
Described flash trapping stage groove is provided with liquid level and flow cascade control system.
Compared with prior art, the invention has the beneficial effects as follows:
1) compared with original technique, the present invention only need to increase several mini-plants and i.e. can reach raising solvent utilization rate, steady
Determine production process, the effect of raising crude benzene refining efficiency, small investment, instant effect, be conducive to improving Business Economic Benefit；
2) technique of the present invention the most additionally increases thermic load, and simple to operate；
3) technique of the present invention the most additionally increases wastewater flow rate, and it is used for giving up after stripping with water all from recovery tower
Water, it is achieved produce cycling utilization of wastewater, arranges outside unharmful substance, and environment protecting is good.
Accompanying drawing explanation
Fig. 1 is the flow chart of solvent regeneration process during crude benzene refining of the present invention.
In figure: 1. blender 1 blender 2 3. flash trapping stage groove 4. blender 3 5. the second-order separation groove 6.
Non-aromatics heavy hydrocarbon component collecting tank 7. water stripper 8. water stripper reboiler 9. solvent regeneration tower 10. solvent reclamation
Tower reboiler
Detailed description of the invention
Below in conjunction with the accompanying drawings the detailed description of the invention of the present invention is described further:
As it is shown in figure 1, solvent regeneration process during a kind of crude benzene refining of the present invention, in normal productive process, through steady
Determine the hydrogenated oil after tower to be directly entered in the middle part of extraction distillation column as extraction feed, enter from the lean solvent come at the bottom of solvent recovery tower
The top of extraction distillation column completes extraction process, non-aromatics with the aromatic hydrocarbons of rising in tower with non-aromatics steam generation phase mass transfer
Enter solvent recovery tower rectification under vacuum from rich solvent at the bottom of overhead extraction, tower, and inject water vapour stripping；At the bottom of solvent recovery tower
Extraction lean solvent, therein 99% returns to extraction distillation column top after cooling recycles, and 1% additionally delivers to solvent again
Raw tower 9 regenerates through steam stripping；Also comprise the steps:
1) the circulation lean solvent entering extraction distillation column is carried out regular pick test, as contained heavy hydrocarbon component content ＞ 3wt%
Time, the lean solvent of extraction at the bottom of solvent recovery tower is no longer sent directly in solvent regeneration tower 9, but first purified process；
2) 1%～2% feeding blender 1 in the circulation lean solvent of extraction distillation column will be entered, and from extractive distillation column overhead
The non-aromatics Product mix of extraction, mixed mixture one sends into blender 22；It is sequentially provided with two-stage after blender 22
Separating tank 3,5, the water drawn bottom the second-order separation groove 5 and solvent mixture also into blender 22, and mix
Thing one is mixed to get mixture two；
3) mixture two enters flash trapping stage groove 3, separated after, water and solvent are miscible and be deposited on flash trapping stage groove 3 times
Portion forms heavy phase, and non-aromatics is dissolved heavy hydrocarbon component and formed light phase on flash trapping stage groove 3 top；Gently, heavy phase layering after, one-level
Separating tank 3 top non-aromatics and the water in heavy hydrocarbon component and solvent recovery tower and benzene distillation tower backflash water shoes are at blender 34
In be sufficiently mixed (wherein containing a small amount of solvent mixture), obtain mixture three；The water of flash trapping stage groove 3 bottom and solvent
Mixture one enters water stripper 7；
4) mixture three enters the second-order separation groove 5, separated after, water and solvent are miscible and be deposited on the second-order separation groove 5 times
Portion forms heavy phase, and non-aromatics is dissolved heavy hydrocarbon component and formed light phase on the second-order separation groove 5 top；Gently, heavy phase layering after, two grades
Separating tank 5 top non-aromatics and heavy hydrocarbon component are delivered to collect in non-aromatics heavy hydrocarbon component collecting tank 6；The second-order separation groove 5 bottom
Water and solvent mixture enter in blender 22；
5) in water stripper 7, after stripping, non-aromatics is isolated from the water in flash trapping stage groove 3 and solvent mixture
Product and water, and obtain purifying lean solvent；Non-aromatics product sends into extractive distillation column overhead, purifies lean solvent through solvent reclamation
Solvent recovery tower is entered after tower 9；
6) as contained heavy hydrocarbon component content≤3wt% in inspection to circulation lean solvent, the lean solvent of extraction at the bottom of solvent recovery tower
The most purified process, is sent directly in solvent regeneration tower 9.
In described blender 1, the mixed volume of lean solvent and non-aromatics product is than for 1:2～3；In blender 22,
Mixture one mixes with arbitrary proportion with water and solvent mixture two；In blender 34, non-aromatics, heavy hydrocarbon component and water with
Arbitrary proportion mixes.
The described mixture two disengaging time in flash trapping stage groove 3, the mixture three disengaging time in the second-order separation groove 5
It is all higher than 4 hours.
Conventional solvents retracting device includes solvent recovery tower, solvent regeneration tower 9 and water stripper, and (in Fig. 1 dotted line frame, part is all
Arrange for routine), the solvent reclamation device of solvent regeneration process during realizing a kind of crude benzene refining of the present invention,
The blender 1 that also includes being sequentially connected with by pipeline, blender 22, flash trapping stage groove 3, blender 34, two fraction
From groove 5 and non-aromatics heavy hydrocarbon component collecting tank 6；Input channel one before blender 1 connects the non-aromatic of extractive distillation tower top
Hydrocarbon product extraction mouth；Input channel two before blender 1 connects the lean solvent outlet of solvent recovery tower；Before blender 22
Input channel three connect the outlet of blender 1, the input channel four before blender 22 connects bottom the second-order separation groove 5
Extraction mouth；The output channel of blender 22 connects the entrance of flash trapping stage groove 3；Input channel five before blender 34 is even
Connecing the top extraction mouth of flash trapping stage groove 3, the input channel six before blender 34 connects solvent recovery tower and benzene distillation tower returns
Chute water shoes；The output channel of blender 34 connects the entrance of the second-order separation groove 5, the top extraction mouth of the second-order separation groove 5
Connect non-aromatics heavy hydrocarbon component collecting tank 6；Bottom flash trapping stage groove 3, extraction mouth connects water stripper 7 entrance.Water stripper
Reboiler 8 is connected by pipeline with solvent regeneration tower reboiler 10.
Described flash trapping stage groove 3 is provided with liquid level and flow cascade control system.
The above, the only present invention preferably detailed description of the invention, but protection scope of the present invention is not limited thereto, and appoints
What those familiar with the art is in the technical scope that the invention discloses, according to technical scheme and send out
Bright design equivalent or change in addition, all should contain within protection scope of the present invention.
Claims (5)
1. a solvent regeneration process during crude benzene refining, in normal productive process, the hydrogenated oil after stabilizer is direct
Enter in the middle part of extraction distillation column as extraction feed, from the lean solvent come at the bottom of solvent recovery tower enter the top of extraction distillation column with
The aromatic hydrocarbons risen in tower and non-aromatics steam generation phase mass transfer complete extraction process, and non-aromatics is from rich at the bottom of overhead extraction, tower
Solvent enters solvent recovery tower rectification under vacuum, and injects water vapour stripping；Extraction lean solvent at the bottom of solvent recovery tower, therein
99% returns to extraction distillation column top after cooling recycles, and 1% additionally is delivered to solvent regeneration tower and regenerated through steam stripping；
It is characterized in that, also comprise the steps:
1) the circulation lean solvent entering extraction distillation column is carried out regular pick test, as contained heavy hydrocarbon component content ＞ 3wt%
Time, the lean solvent of extraction at the bottom of solvent recovery tower is no longer sent directly in solvent regeneration tower, but first purified process；
2) 1%～2% feeding blender one in the circulation lean solvent of extraction distillation column will be entered, and from extractive distillation column overhead
The non-aromatics Product mix of extraction, mixed mixture one sends into blender two；It is sequentially provided with two-stage after blender two to separate
Groove, the water drawn from the second-order separation trench bottom and solvent mixture, also into blender two, are mixed to get mixed with mixture one
Compound two；
3) mixture two enters flash trapping stage groove, separated after, water and solvent are miscible and be deposited on flash trapping stage groove bottom shape
Becoming heavy phase, non-aromatics is dissolved heavy hydrocarbon component and is formed light phase on flash trapping stage groove top；Gently, heavy phase layering after, flash trapping stage groove
Top non-aromatics and the water in heavy hydrocarbon component and solvent recovery tower and benzene distillation tower backflash water shoes are the most mixed in blender three
Close, obtain mixture three；The water of flash trapping stage groove bottom and solvent mixture enter water stripper；
4) mixture three enters the second-order separation groove, separated after, water and solvent are miscible and be deposited on the second-order separation groove bottom shape
Becoming heavy phase, non-aromatics is dissolved heavy hydrocarbon component and is formed light phase on the second-order separation groove top；Gently, heavy phase layering after, the second-order separation groove
Top non-aromatics and heavy hydrocarbon component are delivered to collect in non-aromatics heavy hydrocarbon component collecting tank；The water of the second-order separation groove bottom and solvent mix
Compound enters in blender two；
5) in water stripper, after stripping, non-aromatics product is isolated from the water in flash trapping stage groove and solvent mixture
And water, and obtain purifying lean solvent；Non-aromatics product sends into extractive distillation column overhead, purifies lean solvent after solvent regeneration tower
Enter solvent recovery tower；
6) as contained heavy hydrocarbon component content≤3wt% in inspection to circulation lean solvent, the lean solvent of extraction at the bottom of solvent recovery tower
The most purified process, is sent directly in solvent regeneration tower.
Solvent regeneration process during a kind of crude benzene refining the most according to claim 1, it is characterised in that described mixed
In clutch one, the mixed volume of lean solvent and non-aromatics product is than for 1:2～3；In blender two, mixture one and water and
Solvent mixture mixes with arbitrary proportion；In blender three, the water in non-aromatics, heavy hydrocarbon component and water shoes, a small amount of solvent are mixed
Compound mixes with arbitrary proportion.
Solvent regeneration process during a kind of crude benzene refining the most according to claim 1, it is characterised in that described mixed
The compound two disengaging time in flash trapping stage groove, the mixture three disengaging time in the second-order separation groove are all higher than 4 hours.
4. the solvent reclamation device of solvent regeneration process during realizing a kind of crude benzene refining described in claim 1,
It is characterized in that: the blender one that includes being sequentially connected with by pipeline, blender two, flash trapping stage groove, blender three, two
Level separating tank and non-aromatics heavy hydrocarbon component collecting tank；Input channel one before blender one connects the non-aromatics of extractive distillation tower top
Product extraction mouth；Input channel two before blender one connects the lean solvent outlet of solvent recovery tower；Input before blender two
Pipeline three connects the outlet of blender one, and the input channel four before blender two connects the second-order separation trench bottom extraction mouth；Mixing
The output channel of device two connects the entrance of flash trapping stage groove；Input channel five before blender three connects the top of flash trapping stage groove
Extraction mouth, the input channel six before blender three connects solvent recovery tower and benzene distillation tower backflash water shoes, blender three defeated
Going out pipeline and connect the entrance of the second-order separation groove, the top extraction mouth of the second-order separation groove connects non-aromatics heavy hydrocarbon component collecting tank；One
Level separates trench bottom extraction mouth and connects water stripper entrance.
Solvent reclamation device during a kind of crude benzene refining the most according to claim 4, it is characterised in that described one
Level separating tank is provided with liquid level and flow cascade control system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610585634.7A CN106008457B (en) | 2016-07-21 | 2016-07-21 | Solvent regeneration process and device during a kind of crude benzene refining |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610585634.7A CN106008457B (en) | 2016-07-21 | 2016-07-21 | Solvent regeneration process and device during a kind of crude benzene refining |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106008457A true CN106008457A (en) | 2016-10-12 |
| CN106008457B CN106008457B (en) | 2018-06-22 |
Family
ID=57116334
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610585634.7A Active CN106008457B (en) | 2016-07-21 | 2016-07-21 | Solvent regeneration process and device during a kind of crude benzene refining |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106008457B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106831299A (en) * | 2017-04-01 | 2017-06-13 | 天津奥展兴达化工技术有限公司 | A kind of aromatic hydrocarbons extraction system of efficient energy-saving |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4046641A (en) * | 1974-03-19 | 1977-09-06 | Dr. C. Otto & Comp. G.M.B.H. | Process and apparatus for the separation of crude benzol and naphthalene from washing oil |
| JPS6067438A (en) * | 1983-09-22 | 1985-04-17 | Mitsui Eng & Shipbuild Co Ltd | Recovery of benzene/naphthalene |
| CN103232317A (en) * | 2013-04-05 | 2013-08-07 | 大连理工大学 | Aromatic hydrocarbon purification apparatus and process used in hydrofining of coking crude benzene |
| CN205874268U (en) * | 2016-07-21 | 2017-01-11 | 中冶焦耐(大连)工程技术有限公司 | Thick benzene refining in -process solvent regenerating unit |
-
2016
- 2016-07-21 CN CN201610585634.7A patent/CN106008457B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4046641A (en) * | 1974-03-19 | 1977-09-06 | Dr. C. Otto & Comp. G.M.B.H. | Process and apparatus for the separation of crude benzol and naphthalene from washing oil |
| JPS6067438A (en) * | 1983-09-22 | 1985-04-17 | Mitsui Eng & Shipbuild Co Ltd | Recovery of benzene/naphthalene |
| CN103232317A (en) * | 2013-04-05 | 2013-08-07 | 大连理工大学 | Aromatic hydrocarbon purification apparatus and process used in hydrofining of coking crude benzene |
| CN205874268U (en) * | 2016-07-21 | 2017-01-11 | 中冶焦耐(大连)工程技术有限公司 | Thick benzene refining in -process solvent regenerating unit |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106831299A (en) * | 2017-04-01 | 2017-06-13 | 天津奥展兴达化工技术有限公司 | A kind of aromatic hydrocarbons extraction system of efficient energy-saving |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106008457B (en) | 2018-06-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105777467A (en) | Method for separating oxygenated chemicals and 1-hexene from Fischer-Tropsch synthesis oil product | |
| CN101445420B (en) | Process for preparing benzene aromatic hydrocarbon by crude benzene | |
| KR20010023559A (en) | Aromatics separation process and method retrofitting existing equipment for same | |
| CN102453503B (en) | Method for extracting and separating aromatic hydrocarbon and saturated hydrocarbon in catalytic cracking slurry oil | |
| KR102003498B1 (en) | Regeneration process of polar solvents from aromatic extraction process by treating with light hydrocarbons | |
| CN106278827A (en) | A kind of method and device of extract and separate phenolic compound from coal derived oils | |
| CN105296135B (en) | A kind of regeneration method of waste lubricating oil | |
| CN103073383B (en) | Method and device for separating isohexane, n-hexane and benzene | |
| CN110105159A (en) | The method of separation of extractive distillation aromatic hydrocarbons | |
| CN103086823A (en) | Method and device for separating n-hexane, isohexane and benzene | |
| US2201550A (en) | Process for the solvent extraction of liquid mixtures | |
| TW201345591A (en) | Extraction process with novel solvent regeneration methods | |
| CN102516015A (en) | Production method and system for extracting refined anthracene and carbazole by using crystallization distillation method | |
| CN105255576B (en) | The method and its application of two-stage extraction purification producing base oil by regenerating waste lubricating oil | |
| CN109627140A (en) | A kind of mesitylene extraction and rectification separation method | |
| CN208166931U (en) | The reprocessing system of F- T synthesis diesel oil distillate | |
| CN106008457A (en) | Solvent regenerating process and device for crude benzene refining process | |
| CN205874268U (en) | Thick benzene refining in -process solvent regenerating unit | |
| CN108690658B (en) | Method for recovering aromatic hydrocarbons in low aromatic hydrocarbon content oil | |
| CN105419859A (en) | Reverse back extraction refining method for petroleum reduced pressure distillation distillate and application thereof | |
| RU2680058C2 (en) | Removal of heavy hydrocarbons | |
| US3436435A (en) | Recovery of aromatics | |
| CN209508158U (en) | A kind of extraction distillation tower | |
| CN101157871B (en) | Coal gas naphthalene-purifying waste diesel reclaiming technique | |
| CN105017210B (en) | Regeneration method of sulfolane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |