CN1156751A - Crude oil atmospheric vacuum rectifying process with extractive distillation zone - Google Patents
Crude oil atmospheric vacuum rectifying process with extractive distillation zone Download PDFInfo
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- CN1156751A CN1156751A CN 96101722 CN96101722A CN1156751A CN 1156751 A CN1156751 A CN 1156751A CN 96101722 CN96101722 CN 96101722 CN 96101722 A CN96101722 A CN 96101722A CN 1156751 A CN1156751 A CN 1156751A
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Abstract
An atmospheric vacuum rectifying process for crude oil uses a main apparatus composed of fractional tower, rectifying tower and pressure reducing tower, and features that 4 side pipes are tapped from 4 different positions of fractional tower and directly connected to 4 different positions of rectifying tower, 4 side pipes are tapped from 4 different positions of rectifying tower to obtain 4 different light oil products, and after heated, the liquid from bottom of rectifying tower goes into pressure reducing tower. Compared with available technology, the advantages are decreasing energy consumption by 20-30%, increasing output rate of light oil by 2-3% and high quality of fractional oil.
Description
The invention relates to the normal rectification under vacuum recombination process of crude oil of band stripping section, belong to chemical industry rectifying field.
Crude oil atmospheric distillation and underpressure distillation are collectively referred to as crude oil atmospheric vacuum distillation, are " taps " of refinery, and its effect is the oil content that crude oil is divided into various qualities.The technical process of crude oil atmospheric vacuum distillation can be divided into fuel type according to the purposes difference of product, three kinds of fuel one lubricated oil type and chemical industry types, but basic procedure is similar.Generally partly form by primary tower, atmospheric pressure kiln, atmospheric tower, vacuum furnace, vacuum distillation tower etc.The percentage ratio that the various distillates (except the residual oil) that crude oil obtains through atmospheric and vacuum distillation unit account for the crude oil total amount is called total extracting rate.
Primary tower, atmospheric tower and the vacuum distillation tower of general crude oil atmospheric vacuum distillation device all have only rectifying section and stripping stage, do not have stripping section.Stripping stage is the dividing potential drop that reduces oily vapour by the method that feeds water vapor at the tower still, makes the vaporization of a part of fraction oil.This method needs a large amount of water vapors, and energy consumption is very big.Simultaneously a large amount of water vapors enter the load that has also increased greatly in the tower in the tower, influence the separating effect and the processing power of tower.In addition, the Btu utilization of existing crude oil atmospheric vacuum distillation device is not too reasonable, and the vapour-liquid load distributes very inhomogeneous in the tower.The subject matter of existing crude oil atmospheric vacuum distillation device is that total extracting rate is not too high, and oil quality is not so good, and energy consumption is bigger.
In recent years, energy prices go up very fast, and the cost of crude oil atmospheric vacuum distillation process swashs sharp increase and adds.In order to reduce energy consumption, improve oil quality and total extracting rate, all there is pair crude oil atmospheric vacuum distillation to carry out improved report both at home and abroad.More typically have: change High Efficient Column Internals; Optimize heat exchanger network; Primary tower is opened side line; Primary tower changes flashing tower into; Two atmospheric tower flow processs; Two vacuum distillation tower flow processs etc.These schemes all have certain effect, but not from changing in essence that existing crude oil atmospheric vacuum distillation device has only stripping stage and the shortcoming that do not have stripping section, energy consumption is still than higher.
Fig. 1 is the process flow sheet of two atmospheric tower flow processs in the accompanying drawing.Wherein 1 is interchanger, the 2nd, and atmospheric pressure kiln, 3 is first atmospheric towers, and 4a, 4b are condensers, and 5 is second atmospheric towers, the 6th, vacuum furnace, 7 sufficient crude oil vacuum towers.Crude oil enters 3 flash distillations of first atmospheric tower after interchanger 1 and atmospheric pressure kiln 2 heating.Vapour phase enters rectifying section separates, and obtains overhead oil and sideline product; Liquid phase flows downward and enters atmospheric pressure kiln 2 after the water vapor that feeds at the bottom of the tower contacts, and enters 5 flash distillations of second atmospheric tower after being heated to assigned temperature.The vapour phase that flash distillation produces enters rectifying section separates, and obtains overhead oil and sideline product; Liquid phase flows downward and enters vacuum furnace 6 after the water vapor that feeds at the bottom of the tower contacts, and enters crude oil vacuum tower 7 flash distillations after being heated to assigned temperature.The vapour phase that flash distillation produces enters rectifying section separates, and obtains overhead oil and sideline product; Liquid phase flows downward and contact the back with the water vapor that feeds at the bottom of the tower and give other device processing as residual oil.
First atmospheric tower 3, second atmospheric tower 5 and the crude oil vacuum tower 7 of this pair of atmospheric tower flow process all has only rectifying section and stripping stage and do not have stripping section, goes into water vapor by the tower bottom blowing and produces the stripping effect.The weak point of this technology is: the poor effect of stripping effect, and energy consumption is bigger, and a large amount of water vapors enters not only influences vapour-liquid mass effect in the tower in the tower, influence oil quality, has also increased vapour phase load in the tower greatly, has reduced the processing power of device.The heat of first atmospheric tower 3, second atmospheric tower 5 and crude oil vacuum tower 7 all is disposable adding, and many light components are overheated, and vapour-liquid load skewness needs stage casing backflow heat-obtaining in the tower, and energy consumption is big.First atmospheric tower 3, second atmospheric tower 5 and crude oil vacuum tower 7 are in the stripping stage inferior separating effect, and it is more to contain light component at the bottom of the tower, and the yield of lightweight oil is lower.
The object of the present invention is to provide a kind of energy consumption low, total extracting rate is than higher, the normal rectification under vacuum recombination process of the reasonable crude oil of oil quality, overcome defectives such as above-mentioned technology Btu utilization is unreasonable, energy consumption is high, total extracting rate is lower, reduce the production cost of crude oil atmospheric vacuum distillation device, increase economic efficiency.
Now the present invention is summarized.The present invention is the normal rectification under vacuum recombination process of a kind of crude oil with stripping section, it is characterized in that main body is made up of extraction and distillation of crude oil tower, former oil rectifier and crude oil vacuum tower; The flash overhead that crude oil enters the extraction and distillation of crude oil tower later on through heat exchange, the steam of generation enters the specified location of former oil rectifier; The steam that the unvaporized liquid phase of crude oil flows downward with the tower still rises in the extraction and distillation of crude oil tower contacts and mass transfer, oil returns the extraction and distillation of crude oil tower after heating through atmospheric pressure kiln at the bottom of the extraction and distillation of crude oil Tata, vapour phase upwards flows, and liquid phase goes out through entering crude oil vacuum tower after the vacuum furnace heating from tower bottom flow; Different positions at the extraction and distillation of crude oil tower is extracted four strands of vapour phase side lines out, through being incubated four different positionss that directly enter former oil rectifier; Crude oil rectifying tower top is provided with and is used for the overhead condenser of condensation overhead oil vapour, a phlegma part is back in the tower, with rising vapour phase generation mass transfer, another part extraction is as a kind of clean or white, at four side lines of four different positions extraction of former oil rectifier as different clean or whites; Oil enters crude oil vacuum tower at the bottom of the former oil rectifier tower after the vacuum furnace heating.
In the normal rectification under vacuum recombination process of the crude oil of above-mentioned band stripping section, the tower inner member of said extraction and distillation of crude oil tower is preferably slant-hole tray, also can be column plate or other vapor-liquid contacting apparatus of not being afraid of obstruction.At the bottom of the said extraction and distillation of crude oil Tata gas distributor can be arranged, charging place can have liquid distributor.The charging of extraction and distillation of crude oil tower is at cat head, a certain position that also can be below cat head.
Also can allow at the bottom of the former oil rectifier tower oil at the bottom of the oil and extraction and distillation of crude oil Tata merge after vacuum furnace enters the same position of crude oil vacuum tower after heating.
Sometimes, in order to reduce tower still temperature, also can be blown into a small amount of water vapor at the tower still of extraction and distillation of crude oil tower.
Crude oil vacuum tower of the present invention is preferably a kind of composite crude oil vacuum distillation tower.
Now accompanying drawing of the present invention is described.
Fig. 2 is a process flow diagram of the present invention.8 is the extraction and distillation of crude oil tower among the figure, and 9a, 9b are the tower inner member, 10a, 10b, 10c, 10d are extraction and distillation of crude oil tower vapour phase side line, and 11 is former oil rectifier, 12a, 12b, 12c, 12d, 12e are the extraction of former oil rectifier side line, the 13rd, and oil at the bottom of the former oil rectifier tower, 14 is oil at the bottom of the extraction and distillation of crude oil Tata, and 15 is interchanger, and 16 is atmospheric pressure kiln, 17 is overhead condenser, and 18 is vacuum furnace, and 19 is crude oil vacuum tower.
In conjunction with the accompanying drawings the present invention is described in detail now.
Enter the top of extraction and distillation of crude oil tower 8 after crude oil heats through interchanger 15, the vapour phase that the vaporization back produces enters the specified location of former oil rectifier 11 in the vapour phase mode through extraction and distillation of crude oil tower vapour phase side line 10a; Qi Hua liquid phase does not flow downward, and the vapour phase that produces with the tower still through tower inner member 9a counter current contact heat and mass transport takes place, and light component enters vapour phase, and heavy component enters liquid phase; Specified location extraction extraction and distillation of crude oil tower vapour phase side line 10b at extraction and distillation of crude oil tower 8,10c and 10d directly enter the specified location of former oil rectifier 11, the liquid phase that enters the tower still is returned the tower still after atmospheric pressure kiln 16 is heated to assigned temperature, the vapour phase that vaporization produces upwards flows, not Qi Hua liquid phase as the extraction and distillation of crude oil Tata at the bottom of oil 14 deliver to and enter crude oil vacuum tower 19 after vacuum furnace 18 heats; Through extraction and distillation of crude oil tower vapour phase side line 10b, the vapour phase that 10c, 10d enter former oil rectifier 11 upwards flows, and the liquid that gets off with overhead condenser 17 condensations through tower inner member 9b counter current contact mass-and heat-transfer takes place; Light component enters vapour phase, and heavy component enters liquid phase.Return former oil rectifier 11 as refluxing in the phlegma part that overhead condenser 17 produces, another part is through the normal top of former oil rectifier side line extraction 12a conduct oil.Different positions at former oil rectifier obtains the former extraction of oil rectifier side line 12b, 12c, 12d and 12e.Oil 13 enters crude oil vacuum tower 19 at the bottom of the former oil rectifier tower after pipeline is sent into vacuum furnace 18 heating.Crude oil vacuum tower 19 is operated under reduced pressure.Enter the heavy oil part vaporization of crude oil vacuum tower 19, upwards mobile liquid phase counter current contact of getting off with cat head produces mass-and heat-transfer, and from cat head and the corresponding product of side line extraction.The heavy oil of not vaporizing in crude oil vacuum tower 19 bottoms is given other device as residual oil and is handled.At the bottom of the former oil rectifier tower at the bottom of oil 13 and the extraction and distillation of crude oil Tata oil 14 also can merge after enter the same position of crude oil vacuum tower 19 after the crude oil vacuum furnace heating.
The present invention compares with original crude oil atmospheric vacuum distillation process, and existing rectifying section also has stripping section.The vapour-liquid load distributes more even in the good separating effect of tower, tower.The Btu utilization of whole process is more reasonable, and the oil product of lightweight oil and yield all are higher than original technology.The present invention does not need to feed water vapor basically, has both saved energy consumption, helps improving the processing power of device again, helps vapour-liquid biphase mass transfer yet.
With the Daqing crude oil is example, and we have carried out analog calculation and comparison to the present invention and original technology.Calculation result shows, under identical treatment capacity and identical stage number, the present invention compares with original technology, and energy consumption reduces 20～30%, and the yield of lightweight oil improves 2～3%, and the quality of various fraction oil is all relatively good.
Equipment such as atmospheric pressure kiln of the present invention, vacuum furnace, interchanger, condenser are identical with original technology, but operational condition is different.The structure of extraction and distillation of crude oil tower of the present invention and former oil rectifier is different from original technology, and technical process also has essential distinction.Crude oil enters from carrying the cat head that heats up in a steamer tower, carry through the extraction and distillation of crude oil tower and can guarantee that the light constituent in the crude oil can both volatilize after heating up in a steamer, and the different positions that enters former oil rectifier respectively further separates.Superheating phenomenon can not take place in light constituent, and extraction and distillation of crude oil Tata still also uses no or little water vapor, can save a large amount of energy consumptions.Former oil rectifier further separates the light constituent in the crude oil, can guarantee the oil quality of lightweight oil.This technology is existing than higher yield of light oil, can reduce energy consumption significantly again.
The present invention can be used for the crude oil atmospheric vacuum distillation process, also can be used in the rectifying that other has the mixture of continuous component.
Claims (7)
1. normal rectification under vacuum recombination process of the crude oil with stripping section is characterized in that main body is made up of extraction and distillation of crude oil tower, former oil rectifier and crude oil vacuum tower; The flash overhead that crude oil enters the extraction and distillation of crude oil tower later on through heat exchange, the steam of generation enters the specified location of former oil rectifier; The steam that the unvaporized liquid phase of crude oil flows downward with the tower still rises in the extraction and distillation of crude oil tower contacts and mass transfer, oil returns the extraction and distillation of crude oil tower after heating through atmospheric pressure kiln at the bottom of the extraction and distillation of crude oil Tata, vapour phase upwards flows, and liquid phase goes out through entering crude oil vacuum tower after the vacuum furnace heating from tower bottom flow; Different positions at the extraction and distillation of crude oil tower is extracted four strands of vapour phase side lines out, through being incubated four different positionss that directly enter former oil rectifier; Crude oil rectifying tower top is provided with and is used for the overhead condenser of condensation overhead oil vapour, a phlegma part is back in the tower, with rising vapour phase generation mass transfer, another part extraction is as a kind of clean or white, at four side lines of four different positions extraction of former oil rectifier as different clean or whites; Oil enters crude oil vacuum tower at the bottom of the former oil rectifier tower after the vacuum furnace heating.
2. according to the normal rectification under vacuum recombination process of the said crude oil of claim 1, the tower inner member that it is characterized in that said extraction and distillation of crude oil tower is column plate or other vapor-liquid contacting apparatus of not being afraid of obstruction.
3. according to the normal rectification under vacuum recombination process of the said crude oil of claim 1, the tower inner member that it is characterized in that said extraction and distillation of crude oil tower is a slant-hole tray.
4. according to the normal rectification under vacuum recombination process of the said crude oil of claim 1, it is characterized in that at the bottom of the said extraction and distillation of crude oil Tata gas distributor being arranged, charging place has liquid distributor.
5. according to the normal rectification under vacuum recombination process of the said crude oil of claim 1, it is characterized in that at the bottom of the former oil rectifier tower that oil at the bottom of the oil and extraction and distillation of crude oil Tata merges after vacuum furnace enters the same position of crude oil vacuum tower after heating.
6. according to the normal rectification under vacuum recombination process of the said crude oil of claim 1, it is characterized in that being blown into a small amount of water vapor at the tower still of extraction and distillation of crude oil tower.
7. according to claim 1, the normal rectification under vacuum recombination process of 2,3,4 or 5 said crude oil is characterized in that said crude oil vacuum tower is a kind of composite crude oil vacuum distillation tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96101722A CN1061080C (en) | 1996-02-09 | 1996-02-09 | Crude oil atmospheric vacuum rectifying process with extractive distillation zone |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96101722A CN1061080C (en) | 1996-02-09 | 1996-02-09 | Crude oil atmospheric vacuum rectifying process with extractive distillation zone |
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| Publication Number | Publication Date |
|---|---|
| CN1156751A true CN1156751A (en) | 1997-08-13 |
| CN1061080C CN1061080C (en) | 2001-01-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96101722A Expired - Fee Related CN1061080C (en) | 1996-02-09 | 1996-02-09 | Crude oil atmospheric vacuum rectifying process with extractive distillation zone |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1114458C (en) * | 1999-09-15 | 2003-07-16 | 中国石化上海石油化工股份有限公司 | Crude oil atmospheric vacuum distillation method with deep stripping process |
| CN1313569C (en) * | 2005-06-06 | 2007-05-02 | 周衍亮 | Crude oil full-fraction one-stage reduced pressure distillation process |
| CN100393844C (en) * | 2006-07-10 | 2008-06-11 | 杜小星 | Biodiesel oil multiple-grade molecular distillation process and its device |
| CN106281441A (en) * | 2015-06-08 | 2017-01-04 | 中国石油天然气集团公司 | A kind of crude oil processing technique improving yield of light oil |
| CN106710433A (en) * | 2017-03-22 | 2017-05-24 | 中国石油大学(华东) | Experimental apparatus for atmospheric-vacuum distillation evaluation |
| WO2022029487A1 (en) * | 2020-08-07 | 2022-02-10 | Carbovate Development Corp. | Hydrocarbon stream separation system and method |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5167773A (en) * | 1990-01-16 | 1992-12-01 | Exxon Research And Engineering Co. | Distillation tower and sidestream stripper therefor |
| CN1020257C (en) * | 1991-03-07 | 1993-04-14 | 天津大学 | Multistage flash and rectification coupling technology |
-
1996
- 1996-02-09 CN CN96101722A patent/CN1061080C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1114458C (en) * | 1999-09-15 | 2003-07-16 | 中国石化上海石油化工股份有限公司 | Crude oil atmospheric vacuum distillation method with deep stripping process |
| CN1313569C (en) * | 2005-06-06 | 2007-05-02 | 周衍亮 | Crude oil full-fraction one-stage reduced pressure distillation process |
| CN100393844C (en) * | 2006-07-10 | 2008-06-11 | 杜小星 | Biodiesel oil multiple-grade molecular distillation process and its device |
| CN106281441A (en) * | 2015-06-08 | 2017-01-04 | 中国石油天然气集团公司 | A kind of crude oil processing technique improving yield of light oil |
| CN106710433A (en) * | 2017-03-22 | 2017-05-24 | 中国石油大学(华东) | Experimental apparatus for atmospheric-vacuum distillation evaluation |
| CN106710433B (en) * | 2017-03-22 | 2023-11-17 | 中国石油大学(华东) | Experimental device for evaluation is pulled out deeply to atmospheric and vacuum pressure |
| WO2022029487A1 (en) * | 2020-08-07 | 2022-02-10 | Carbovate Development Corp. | Hydrocarbon stream separation system and method |
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| Publication number | Publication date |
|---|---|
| CN1061080C (en) | 2001-01-24 |
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