CN101586037A - Method for realizing selective reprocessing of catalytic cracking reprocessed oil slurry - Google Patents
Method for realizing selective reprocessing of catalytic cracking reprocessed oil slurry Download PDFInfo
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- CN101586037A CN101586037A CNA2009100122173A CN200910012217A CN101586037A CN 101586037 A CN101586037 A CN 101586037A CN A2009100122173 A CNA2009100122173 A CN A2009100122173A CN 200910012217 A CN200910012217 A CN 200910012217A CN 101586037 A CN101586037 A CN 101586037A
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- catalytic cracking
- oil slurry
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- reprocessed oil
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Abstract
The invention discloses a method for realizing selective reprocessing of catalytic cracking reprocessed oil slurry. The method comprises the steps of conveying reprocessed oil slurry produced by a catalytic cracking device into a reduced-pressure rectification column for rectification under reduced pressure, separating out low-carbon-residue fractions of which the boiling point is lower than 500 to 550 DEG C and sending the low-carbon-residue fractions to a reprocessing device. The method first performs reduced-pressure rectification on the reprocessed oil slurry produced by the catalytic cracking device through the reduced-pressure rectification column, then separates the low-carbon-residue fractions out from the reprocessed oil slurry, and sends the low-carbon-residue fractions to the reprocessing device. Because high-carbon-residue fractions do not enter the reprocessing device, the occurrence of coke generation of the reprocessing device is fundamentally avoided; the processing capacity of the device is improved; the energy consumption and maintenance cost of the device are reduced; and the energy consumption of the device can be reduced by more than 10 percent. In addition, the method also greatly reduces processing loss and increases the yield of lightweight oil by about 1 to 3 percent, thereby having significant economic benefit.
Description
One, technical field
The invention belongs to the petrochemical technology field, be specifically related to a kind of method that realizes selective reprocessing of catalytic cracking reprocessed oil slurry.
Two, background technology
At present, in the existing petroleum refining process technology, catalytic cracking unit is occupied critical role as the important means of oil secondary processing in each refinery.In the catalytic cracking production process, bottom of device can produce a large amount of slurry oils, and this part slurry oil is delivered to as reprocessed oil slurry usually and carried out the freshening recovery in the freshening device.Reprocessed oil slurry generally by boiling point greater than 500-550 ℃ high carbon residue cut and boiling point low carbon residue fractions consisting less than 500-550 ℃, every kind of cut accounts for about 50%.Its mid-boiling point because carbon residue is higher, very easily causes freshening device green coke greater than 500-550 ℃ cut, has not only increased the energy consumption and the maintenance cost of device, and has reduced the working ability of device, has increased refining losses, has greatly influenced economic benefit.
Three, summary of the invention
The purpose of this invention is to provide a kind of method that realizes selective reprocessing of catalytic cracking reprocessed oil slurry, adopt this method can avoid freshening device green coke effectively, reduce the energy consumption and the maintenance cost of device, reduce refining losses, increase economic efficiency.
For achieving the above object, the technical solution used in the present invention is: this method is as follows: the reprocessed oil slurry that catalytic cracking unit is produced is delivered in the rectification under vacuum tower, carry out rectification under vacuum, its mid-boiling point is separated less than 500-550 ℃ low carbon residue cut delivered to the freshening device.
Described rectification under vacuum tower operating pressure is 50-100kPa.
Described rectification under vacuum column overhead temperature is 40-150 ℃.
The inventive method is that the reprocessed oil slurry that catalytic cracking unit produces is carried out rectification under vacuum through the rectification under vacuum tower earlier, will wherein hang down carbon residue and heat up in a steamer to separate in the reprocessed oil slurry and deliver to the freshening device.Because high carbon residue cut does not enter the freshening device, has fundamentally avoided the generation of freshening device green coke, improve the working ability of device, reduced the energy consumption and the maintenance cost of device, the energy consumption of device can reduce more than 10%.Simultaneously, refining losses is also reduced greatly, makes yield of light oil improve about 1-3% remarkable in economical benefits.The inventive method be utilize first rectifying again the mode of freshening realized selective reprocessing to reprocessed oil slurry, not only simple, and facility investment is low, and can realize serialization production.
Four, description of drawings
Accompanying drawing is a process flow sheet of the present invention.
Five, embodiment
Shown in the figure of institute, the catalytic cracking unit that the present invention adopts is a catalytic rectifying tower, it is interior behind catalytic distillation that reaction oil gas enters tower, output rich gas and gasoline and solar oil respectively from cat head and tower middle part, at the bottom of the tower output by boiling point greater than 500-550 ℃ high carbon residue cut and boiling point less than 500-550 ℃ low carbon residue fractions consisting, temperature is 340-390 ℃ reprocessed oil slurry; This reprocessed oil slurry through pipeline is delivered to the rectification under vacuum tower that cat head has pumped vacuum systems with pump in, is entered feed zone through rectification under vacuum tower feed distributor, carry out rectification under vacuum.Its mid-boiling point is less than 500-550 ℃ low carbon residue cut, and vaporization and flow out from each side line 1,2,3 that is located in the rectification under vacuum under certain negative pressure is delivered to riser reactor through pipeline with pump and carries out freshening.From the effusive low carbon residue cut temperature of each side line is 60-350 ℃; Boiling point flows into the rectification under vacuum tower bottom greater than 500-550 ℃ high carbon residue cut, carries by pump through pipeline, and storage tank outside after the water cooler cooling, sending into again, as oil fuel or other industrial chemicals, it goes out the flash-point that unit temp is not more than this cut.Side line quantity on the above-mentioned rectification under vacuum tower can be generally 2-5 according to the design of actual process needs.Above-mentioned rectification under vacuum tower operating pressure is 50-100kPa.Above-mentioned rectification under vacuum column overhead temperature is 40-150 ℃.The effect of above-mentioned rectification under vacuum top of tower pumped vacuum systems is the non-condensable gas of extracting out in the tower, forms certain negative pressure.Above-mentioned rectification under vacuum tower can be provided with the pump around circuit system according to the actual process needs.Each pump around circuit system is made up of pump, instrument control valve, interchanger, water cooler, pipeline and valve etc.Above-mentioned rectification under vacuum tower inside is provided with feed distributor, distribution of reflux device, tower tray or filler, oil header.Above-mentioned rectification under vacuum tower outside is provided with opening for feed, cat head gas phase spout and tower bottom outlet.
Claims (3)
1, a kind of method that realizes selective reprocessing of catalytic cracking reprocessed oil slurry, it is characterized in that: this method is delivered in the rectification under vacuum tower for the reprocessed oil slurry that catalytic cracking unit is produced, carry out rectification under vacuum, its mid-boiling point is separated less than 500-550 ℃ low carbon residue cut delivered to the freshening device.
2, according to right 1 described described a kind of method that realizes selective reprocessing of catalytic cracking reprocessed oil slurry, it is characterized in that: described rectification under vacuum tower operating pressure is 50-100kPa.
3, according to right 1 or 2 described described a kind of methods that realize selective reprocessing of catalytic cracking reprocessed oil slurry, it is characterized in that: described rectification under vacuum column overhead temperature is 40-150 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100122173A CN101586037A (en) | 2009-06-25 | 2009-06-25 | Method for realizing selective reprocessing of catalytic cracking reprocessed oil slurry |
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| Application Number | Priority Date | Filing Date | Title |
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| CNA2009100122173A CN101586037A (en) | 2009-06-25 | 2009-06-25 | Method for realizing selective reprocessing of catalytic cracking reprocessed oil slurry |
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| CN101586037A true CN101586037A (en) | 2009-11-25 |
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| CNA2009100122173A Pending CN101586037A (en) | 2009-06-25 | 2009-06-25 | Method for realizing selective reprocessing of catalytic cracking reprocessed oil slurry |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102102029A (en) * | 2009-12-17 | 2011-06-22 | 中国石油大学(北京) | Catalytic cracking fractional and divisional transformation method and device for heavy oil |
| CN102102026A (en) * | 2009-12-17 | 2011-06-22 | 中国石油大学(北京) | Method and device for heavy oil tandem regional catalytic cracking |
| CN102234531A (en) * | 2010-05-06 | 2011-11-09 | 中国石油天然气股份有限公司 | Device for catalytically cracking heavy oil in sections and application thereof |
| CN102234532A (en) * | 2010-05-06 | 2011-11-09 | 中国石油天然气股份有限公司 | Series-connected, partitioned and classified method and apparatus for catalytic cracking of heavy oil |
| CN102102028B (en) * | 2009-12-17 | 2014-01-22 | 中国石油大学(北京) | Fractional and divisional catalytic cracking method and device for heavy oil |
| CN102102030B (en) * | 2009-12-17 | 2014-01-22 | 中国石油大学(北京) | Heavy oil catalytic cracking method and device by double-area coupling and catalyst tandem |
| CN102102027B (en) * | 2009-12-17 | 2014-04-02 | 中国石油大学(北京) | Heavy oil serial graded and zoned catalytic conversion method and device |
| CN102102025B (en) * | 2009-12-17 | 2014-04-02 | 中国石油大学(北京) | Heavy oil serial/parallel multi-area catalytic cracking method and device |
-
2009
- 2009-06-25 CN CNA2009100122173A patent/CN101586037A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102102029A (en) * | 2009-12-17 | 2011-06-22 | 中国石油大学(北京) | Catalytic cracking fractional and divisional transformation method and device for heavy oil |
| CN102102026A (en) * | 2009-12-17 | 2011-06-22 | 中国石油大学(北京) | Method and device for heavy oil tandem regional catalytic cracking |
| CN102102029B (en) * | 2009-12-17 | 2014-01-22 | 中国石油大学(北京) | Catalytic cracking fractional and divisional transformation method and device for heavy oil |
| CN102102028B (en) * | 2009-12-17 | 2014-01-22 | 中国石油大学(北京) | Fractional and divisional catalytic cracking method and device for heavy oil |
| CN102102030B (en) * | 2009-12-17 | 2014-01-22 | 中国石油大学(北京) | Heavy oil catalytic cracking method and device by double-area coupling and catalyst tandem |
| CN102102027B (en) * | 2009-12-17 | 2014-04-02 | 中国石油大学(北京) | Heavy oil serial graded and zoned catalytic conversion method and device |
| CN102102025B (en) * | 2009-12-17 | 2014-04-02 | 中国石油大学(北京) | Heavy oil serial/parallel multi-area catalytic cracking method and device |
| CN102234531A (en) * | 2010-05-06 | 2011-11-09 | 中国石油天然气股份有限公司 | Device for catalytically cracking heavy oil in sections and application thereof |
| CN102234532A (en) * | 2010-05-06 | 2011-11-09 | 中国石油天然气股份有限公司 | Series-connected, partitioned and classified method and apparatus for catalytic cracking of heavy oil |
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Application publication date: 20091125 |