CN1470607A - Catalytic hydrocarbon reforming treatment method - Google Patents
Catalytic hydrocarbon reforming treatment method Download PDFInfo
- Publication number
- CN1470607A CN1470607A CNA031481817A CN03148181A CN1470607A CN 1470607 A CN1470607 A CN 1470607A CN A031481817 A CNA031481817 A CN A031481817A CN 03148181 A CN03148181 A CN 03148181A CN 1470607 A CN1470607 A CN 1470607A
- Authority
- CN
- China
- Prior art keywords
- gasoline
- diesel oil
- separation column
- fractionation
- boiling range
- 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
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 62
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 51
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 51
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000002407 reforming Methods 0.000 title 1
- 239000003502 gasoline Substances 0.000 claims abstract description 157
- 239000002283 diesel fuel Substances 0.000 claims abstract description 123
- 238000005194 fractionation Methods 0.000 claims abstract description 65
- 238000000605 extraction Methods 0.000 claims abstract description 44
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims abstract description 28
- 230000008569 process Effects 0.000 claims abstract description 21
- 238000002156 mixing Methods 0.000 claims abstract description 14
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 claims abstract description 8
- 238000000926 separation method Methods 0.000 claims description 89
- 238000009835 boiling Methods 0.000 claims description 65
- 239000003921 oil Substances 0.000 claims description 51
- 125000003118 aryl group Chemical group 0.000 claims description 40
- 230000009183 running Effects 0.000 claims description 34
- 239000000126 substance Substances 0.000 claims description 34
- 230000008521 reorganization Effects 0.000 claims description 15
- 238000000638 solvent extraction Methods 0.000 claims description 8
- 238000005345 coagulation Methods 0.000 claims description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 7
- 238000005215 recombination Methods 0.000 abstract 1
- 230000006798 recombination Effects 0.000 abstract 1
- 230000000052 comparative effect Effects 0.000 description 31
- 239000002904 solvent Substances 0.000 description 31
- 239000003054 catalyst Substances 0.000 description 28
- 239000007789 gas Substances 0.000 description 27
- 239000000295 fuel oil Substances 0.000 description 20
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 18
- 150000001336 alkenes Chemical class 0.000 description 17
- 238000007599 discharging Methods 0.000 description 17
- 239000002994 raw material Substances 0.000 description 16
- 238000004519 manufacturing process Methods 0.000 description 14
- 230000009471 action Effects 0.000 description 12
- 238000004821 distillation Methods 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 8
- 241000282326 Felis catus Species 0.000 description 6
- 239000000571 coke Substances 0.000 description 6
- 238000005984 hydrogenation reaction Methods 0.000 description 6
- 239000002002 slurry Substances 0.000 description 6
- 238000004523 catalytic cracking Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 4
- 238000010276 construction Methods 0.000 description 4
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 3
- 125000000753 cycloalkyl group Chemical group 0.000 description 3
- 238000004231 fluid catalytic cracking Methods 0.000 description 3
- UWHCKJMYHZGTIT-UHFFFAOYSA-N tetraethylene glycol Chemical compound OCCOCCOCCOCCO UWHCKJMYHZGTIT-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 2
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 description 2
- 229920000728 polyester Polymers 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000011218 segmentation Effects 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- -1 alkane ketone Chemical class 0.000 description 1
- 150000001408 amides Chemical class 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002334 glycols Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 150000003457 sulfones Chemical class 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention discloses a catalytic hydrocarbon recombination treatment method, which includes: making the catalytic hydrocarbon pass through catalytic main fractionator to implement fractionation to obtain gasoline fraction and diesel oil fraction, adding an intermediate fraction, making said described intermediate fraction undergo the process of aromatic hydrocarbon extraction treatment to obtain aromatic hydrocarbon component and non-aromatic hydrocarbon component; fractionating aromatic hydrocarbon component and mixing the obtained high octane value gasoline component with the gasoline fraction to raise the octane value of gasoline; fractionating non-aromatic hydrocarbon component and mixing the obtained diesel oil component and diesel oil fraction to raise diesel oil yield and its cetane value.
Description
Technical field
The present invention relates to a kind of catalytic hydrocarbon reorganization treatment process, the treatment process of particularly a kind of catalyzing hydrocarbon for recombinant production of high-quality gasoline, diesel oil and chemical industry light oil.
Background technology
Catalytic cracking, catalytic pyrolysis and heavy oil catalytic pyrolysis technology are the core technologies of oil refining, and catalytic cracking is divided into wax catalysis cracking, heavy oil fluid catalytic cracking; The oil gas that generates from the reaction-regeneration system of these technologies is referred to as catalytic hydrocarbon, and the gained catalytic hydrocarbon generally is the main fractionating tower fractionation through processing treatment, can fractionate out products such as dry gas, liquefied gas, gasoline, diesel oil, heavy oil.
More and more strictness along with environmental requirement, the standard of gasoline, diesel oil improves constantly, existing catalytic hydrocarbon is showed following deficiency through the fractionated processing and treating method of separation column: one is that the gasoline produced of this treatment process and the quality of diesel oil have much room for improvement: the olefin(e) centent of gasoline is higher, octane value is on the low side, and diesel-fuel cetane number is on the low side; The 2nd, above-mentioned treatment process can not be produced the gasoline of multiple label simultaneously, and range of product is single; The 3rd, the demand in the diesel oil of being produced, the ratio of gasoline and market does not match, and diesel oil can not satisfy the demands, and gasoline supply exceed demand.
The principal element that influences gasoline product quality is the olefin(e) centent of gasoline and the octane value of gasoline.At present, oil refining enterprise takes to increase the measure of gasoline octane rating: 1. increase high octane value gasoline blending component, generate oil, isomerization generation wet goods as reformed oil, alkylate oil, etherificate; 2. adopt new catalyst; 3. adjust the Hydrocarbon Content by Catalytic Cracking Operation condition; 4. adjust gasoline boiling range scope.
There is following point in above-mentioned measure: the restriction that 1. construction investment is huge, process cost is high, scale is subjected to raw material, the irrational utilization that has resource simultaneously, as reformed oil is the main raw material of producing polyester, a large amount of reformed oils are used for high octane value gasoline blending component, have then aggravated original just polyester raw material degree in short supply very in short supply; 2. adopt new catalyst, can increase the octane value of gasoline, still, can cause olefin content in gasoline to increase considerably, diesel and gasoline ratio reduces; 3. adjust the Hydrocarbon Content by Catalytic Cracking Operation condition, increase the measure of gasoline octane rating, can cause olefin content in gasoline to increase equally, diesel and gasoline ratio reduces; 4. adjust gasoline boiling range scope, increase the measure of gasoline octane rating, it is little to adjust remaining, also can cause olefin content in gasoline to increase.All by the measure that increases alkene and increase gasoline octane rating all with to carry out new gasoline standard inconsistent.
At present, the measure of taking to reduce alkene mainly is: 1. adopt olefine lowering catalyst; 2. the catalytic gasoline segmentation is carried out hydrogenation and non-hydrotreatment; 3. adopt gasoline freshening technology such as double lifting leg.
There is following point in above-mentioned measure: 1. adopt olefine lowering catalyst, can cause gasoline octane rating obviously to reduce; 2. hydrogenation and non-hydrotreatment technology are carried out in the catalytic gasoline segmentation, though can reduce olefin(e) centent, the octane value of gasoline does not increase, and this technological investment is bigger, is subjected to the restriction of hydrogen resource simultaneously; 3. adopt gasoline freshening technology such as double lifting leg, it is limited to reduce the alkene amplitude, and this technical innovation project and technical difficulty are bigger, and the octane value of gasoline does not increase simultaneously.
Diesel-fuel cetane number is the key problem of diesel quality, the major measure that increases the catalytic diesel oil cetane value at present is high-pressure hydrogenation and high-pressure hydrogenation combination technique, catalytic diesel oil cetane value after high-pressure hydrogenation and the processing of high-pressure hydrogenation combination technique has a more substantial increase, but the construction investment of this technology is huge, running cost is very high, be subjected to the hydrogen resource limit.
Summary of the invention
One of purpose of the present invention provides a kind of catalytic hydrocarbon reorganization treatment process, preparation high quality vapour axle and diesel oil.
Further purpose of the present invention is by the catalytic hydrocarbon reorganization, produces the gasoline and the diesel oil of various labels simultaneously, also can increase products such as chemical industry light oil, heavy aromatics.
Other purpose of the present invention is to improve diesel and gasoline ratio, meets the need of market.
For achieving the above object, the present invention takes following technical scheme:
A kind of catalytic hydrocarbon reorganization treatment process is carried out fractionation with catalytic hydrocarbon by separation column 1, comprising fractionation gasoline fraction and diesel oil distillate; It is characterized in that: gasoline fraction and diesel oil distillate are reconfigured, between described gasoline fraction and diesel oil distillate, extract middle runnings out; Again extracting and separating is carried out in described middle runnings in solvent extraction plant, isolate aromatic component and non-aromatic component.
A kind of preferred version, it is characterized in that: fractionate out middle runnings by increase one or more side line extraction mouths at separation column 1 middle part, the tower top temperature of separation column 1 is 65～130 ℃, the diesel oil temperature out is 170～250 ℃, side line extraction mouth temperature is 120～240 ℃, and column bottom temperature is 330～385 ℃; The tower top pressure of separation column 1 is 0.15～0.28MPa, and tower bottom pressure is 0.12～0.30MPa; Described gasoline fraction and diesel oil distillate and middle runnings are finished in described separation column 1; The boiling range of described gasoline fraction is controlled at 35～150 ℃, and the boiling range of described diesel oil distillate is controlled at 170～395 ℃, and the boiling range of described middle runnings is controlled at 70～250 ℃.
A kind of preferred version, it is characterized in that: described fractionation is two step fractionation, the first step, elder generation's fractionation gasoline fraction and diesel oil distillate, the temperature of separation column 1 top and diesel oil extraction mouth is improved 10～50 ℃, the boiling range of described gasoline fraction is controlled at 35～250 ℃, and the boiling range of diesel oil distillate is controlled at 170～395 ℃; Described gasoline fraction pumps into separation column 2, carries out the fractionation second time, and it is 70 ℃～250 ℃ middle runnings that described separation column 2 bottom side lines are isolated boiling range, and it is 35～150 ℃ gasoline fraction that its top distills out boiling range.
A kind of preferred version, it is characterized in that: described fractionation is two step fractionation, the first step, elder generation's fractionation gasoline fraction and diesel oil distillate, the temperature of separation column 1 top and diesel oil extraction mouth is reduced by 10～50 ℃, the boiling range of described gasoline fraction is controlled at 35～150 ℃, and the boiling range of diesel oil distillate is controlled at 70～395 ℃; Described diesel oil distillate pumps into separation column 5, carries out the fractionation second time, and described separation column 5 bottom side line extraction boiling ranges are 170～395 ℃ diesel oil distillate, and it is 70～250 ℃ middle runnings that its top distills out boiling range.
A kind of preferred version, it is characterized in that: described aromatic component and solvent are entered carry out fractionation in the separation column 3, described separation column 3 tops distill out high octane gasoline component, its underpart side line extraction heavy aromatics component, gained high octane gasoline component and boiling range are 35～150 ℃ of gasoline fraction blendings.
A kind of preferred version is characterized in that: described high octane gasoline component can be that 35～150 ℃ gasoline fraction is all concocted with described boiling range.
A kind of preferred version is characterized in that: described high octane gasoline component and described boiling range are that 35～150 ℃ gasoline fraction is concocted according to set(ting)value, obtain the gasoline of different labels, as 90# gasoline, 93# gasoline, 97# gasoline etc.
A kind of preferred version is characterized in that: described fractionated process of a step, can draw 1 to 4 side line extraction mouth in separation column 1 middle runnings, and make middle runnings be divided into 1 to 4 logistics.
A kind of preferred version, it is characterized in that: described non-aromatic component carries out fractionation in separation column 4, described separation column 4 bottom side line extraction diesel components, and with itself and described boiling range 170～380 ℃ diesel oil distillate blending, improve diesel-fuel cetane number, also can concoct out one or more low-coagulation diesel oils and non-low-coagulation diesel oil according to market situation; Light non-aromatics is isolated at described separation column 4 tops, and this light non-aromatics can be used as chemical industry light oil, also can concoct with gasoline fraction.
The aromaticity content of gained chemical industry light oil is very low, after hydrofining, can be used as the high quality raw material of cracking of ethylene.
Described aromatic component also can directly use as premium-type gasoline.
The extraction solvent for use can be sulfone class such as tetramethylene sulfone, glycols such as Tetraglycol 99 and five glycol, and alkane ketone such as N-Methyl pyrrolidone, amides and amine etc. also can two or more solvent use.
Advantage of the present invention is: the product that the inventive method is produced does not have other blending component to participate in all only from catalytic cracking fractionating tower gasoline and diesel oil distillate; Reduce the yield of gasoline; Aromaticity content improves in the gasoline, makes Study of Gasoline method octane value improve 2～5 units; The boiling range of gasoline broadens, and becomes 35～203 ℃ by 35～190 ℃; The yield of diesel oil has increased by 5～7 units; Diesel and gasoline ratio has improved 0.4～0.8; The aromaticity content of diesel oil reduces, and makes its cetane value improve 5～7 units; The boiling range scope of diesel oil broadens, and becomes 165～365 ℃ by 180～365 ℃; Diesel-fuel flash point reduces, and becomes 56 ℃ by 75 ℃; High-quality chemical industry light oil products and heavy aromatics product have been increased; Because aromatic hydrocarbons, the non-aromatics of petrol and diesel oil middle runnings are come out, can access 90#, 93# and the 97# gasoline of different ratios after the high-octane number component of aromatic component and the gasoline fraction blending, factory can adjust production decision flexibly according to market situation; The inventive method can make catalytic gasoline after not needing the high-octane number component blending, just can directly dispatch from the factory, and has saved high-octane number component, and particularly reformed oil is again the main source of light aromatic hydrocarbons; Compare with other method, the inventive method only need be on the basis of original catalytic hydrocarbon device, increase an extraction tower and several separation columns, can realize improving the quality of gasoline and diesel oil, can also produce the gasoline and the diesel oil of different labels simultaneously, construction investment is little, the construction period is short, simple to operate, process cost is low; Can improve the present situation that diesel and gasoline ratio can not be satisfied the demand within a short period of time.
Description of drawings
Fig. 1 is the schematic flow sheet of one embodiment of the invention;
Fig. 2 is the schematic flow sheet of another embodiment of the present invention;
Fig. 3 is the schematic flow sheet of further embodiment of this invention.
Accompanying drawing is the synoptic diagram of catalytic hydrocarbon reorganization treating processes of the present invention, and some utility appliance among the figure such as separating tank, pump, various cold exchange devices etc. do not mark, but this is known to those of ordinary skills.
The present invention will be further described below by embodiment, but and do not mean that limiting the scope of the invention.
Embodiment
Comparative Examples 1
Paraffinic base fcc raw material and recycle stock are produced catalytic hydrocarbon under the LCS catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 110 ℃, the diesel oil temperature out is 190 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.11MPa, and tower bottom pressure is 0.12MPa, and fractionation obtains dry gas, liquefied gas, gasoline, diesel oil, heavy oil fraction etc.
As shown in Figure 1, paraffinic base fcc raw material and recycle stock are produced catalytic hydrocarbon under the LCS catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 80 ℃, the diesel oil temperature out is 240 ℃, column bottom temperature is 370 ℃, and tower top pressure is 0.1MPa, and tower bottom pressure is 0.12Mpa; Middle part at separation column 1 increases a side line extraction mouth, be used to cut middle runnings, side line extraction mouth temperature is 190 ℃, the boiling range scope of middle runnings is 120～210 ℃, and gained middle runnings pumps into extraction plant and carries out solvent extraction and separation, and solvent for use is a tetramethylene sulfone, extraction temperature is 80 ℃, extracting pressure is 0.4MPa, and weight of solvent is 4.8 than (solvent/charging), isolates aromatic component and non-aromatic component; Gained aromatic component and solvent enter in the separation column 3 in the middle part, carry out fractionation by distillation, cut point is 120～165 ℃, fractionation pressure is 0.04～0.20MPa, bottom admission water lift, overhead fraction is a high-octane number component, the bottom side line extraction mouth aromatic component of attaching most importance to, and discharging is as circulating solvent at the bottom of the tower; The gained high-octane number component is all concocted with gasoline fraction; The gained non-aromatic component enters in the separation column 4 in the middle part, carries out fractionation by distillation, and cut point is 100～135 ℃, and pressure is 0.15～0.25MPa, and the cat head discharging is light non-aromatics, and discharging is a diesel component at the bottom of the tower; The gained diesel component is all concocted with diesel oil distillate; Light non-aromatics of gained and gasoline fraction blending.
Comparative Examples 2
Intermediate base normal slag heavy-oil catalytic raw material and recycle stock are produced catalytic hydrocarbon under the LANET-35 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 110 ℃, the diesel oil temperature out is 190 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.11MPa, and tower bottom pressure is 0.12MPa, and fractionation obtains dry gas, liquefied gas, gasoline, diesel oil, heavy oil fraction etc.
Intermediate base normal slag heavy-oil catalytic raw material and recycle stock are produced catalytic hydrocarbon under the LANET-35 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 80 ℃, the diesel oil temperature out is 240 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.1MPa, and tower bottom pressure is 0.12Mpa; Middle part at separation column 1 increases by three side line extraction mouths, be used to cut middle runnings, three side line extraction mouth temperature are followed successively by 170,180,190 ℃ from top to bottom, the boiling range scope of middle runnings is respectively 80～120 ℃, 120～165 ℃, 155～220 ℃, the middle runnings of three boiling ranges of gained pumps into three identical extraction plants and carries out solvent extraction and separation, solvent for use is a Tetraglycol 99, extraction temperature is 85 ℃, extracting pressure is 0.4MPa, weight of solvent is 3.1 than (solvent/charging), isolates aromatic component and non-aromatic component; The gained aromatic component merges the back and solvent enters in the separation column 3 in the middle part, carry out fractionation by distillation, cut point is 120～180 ℃, fractionation pressure is 0.04～0.20MPa, bottom admission water lift, overhead fraction is a high-octane number component, the bottom side line extraction mouth aromatic component of attaching most importance to, and discharging is as circulating solvent at the bottom of the tower; The gained high-octane number component is all concocted with gasoline fraction; The gained non-aromatic component merges the back and enters in the separation column 4 in the middle part, carries out fractionation by distillation, and cut point is 100～135 ℃, and pressure is 0.15～0.25MPa, and the cat head discharging is light non-aromatics, and discharging is a diesel component at the bottom of the tower; The gained diesel component is all concocted with diesel oil distillate; Light non-aromatics of gained and gasoline fraction blending.
Comparative Examples 3
Cycloalkyl heavy-oil catalytic raw material and recycle stock are produced catalytic hydrocarbon under the LANET-35 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 110 ℃, the diesel oil temperature out is 190 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.11MPa, and tower bottom pressure is 0.12MPa, and fractionation obtains dry gas, liquefied gas, gasoline, diesel oil, heavy oil fraction etc.
Cycloalkyl heavy-oil catalytic raw material and recycle stock are produced catalytic hydrocarbon under the LANET-35 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 80 ℃, the diesel oil temperature out is 240 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.18MPa, and tower bottom pressure is 0.25Mpa; Middle part at separation column 1 increases by two side line extraction mouths, be used to cut middle runnings, two side line extraction mouth temperature are followed successively by 180,190 ℃ from top to bottom, the boiling range scope of middle runnings is respectively 80～165 ℃, 165～220 ℃, the middle runnings of two boiling ranges of gained is carried out solvent extraction and separation pumping into two identical extraction plants, solvent for use is the N-formyl morpholine, extraction temperature is 85 ℃, extracting pressure is 0.4MPa, weight of solvent is 3.1 than (solvent/charging), isolates aromatic component and non-aromatic component; The gained aromatic component merges the back and enters in the separation column 3 in the middle part, carry out fractionation by distillation, cut point is 120～180 ℃, fractionation pressure is 0.04～0.20MPa, bottom admission water lift, overhead fraction is a high-octane number component, the bottom side line extraction mouth aromatic component of attaching most importance to, and discharging is as circulating solvent at the bottom of the tower; The gained high-octane number component is all concocted with gasoline fraction; The gained non-aromatic component merges the back and solvent enters in the separation column 4 in the middle part, carries out fractionation by distillation, and cut point is 100～135 ℃, and pressure is 0.15～0.25MPa, and the cat head discharging is light non-aromatics, and discharging is a diesel component at the bottom of the tower; The gained diesel component is all concocted with diesel oil distillate; The light non-aromatics of gained is used as chemical industry light oil.
Comparative Examples 4
Paraffinic base heavy-oil catalytic raw material and recycle stock are produced catalytic hydrocarbon under the LBO-16 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 110 ℃, the diesel oil temperature out is 190 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.11MPa, and tower bottom pressure is 0.12MPa, and fractionation obtains dry gas, liquefied gas, gasoline, diesel oil, heavy oil fraction etc.
Embodiment 4
As shown in Figure 3, paraffinic base heavy oil fluid catalytic cracking raw material and recycle stock are produced catalytic hydrocarbon under the LBO-16 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 90 ℃, and the diesel oil temperature out is 180 ℃, and column bottom temperature is 340 ℃, tower top pressure is 0.1MPa, tower bottom pressure is 0.12Mpa, and the boiling range of described gasoline fraction is controlled at 35～120 ℃, and the boiling range of diesel oil distillate 1 is controlled at 120～355 ℃; Described diesel oil distillate 1 pumps into separation column 2, carry out the fractionation second time, separation column 2 tower top temperatures are 80 ℃, the diesel oil temperature out is 240 ℃, column bottom temperature is 370 ℃, and tower top pressure is 0.1MPa, and tower bottom pressure is 0.12Mpa, it is 80 ℃～240 ℃ middle runnings that boiling range is isolated at described separation column 2 tops, and it is 240～380 ℃ gasoline fraction that boiling range is isolated in its bottom.Middle runnings pumps into extraction plant and carries out solvent extraction and separation, and solvent for use is a N-Methyl pyrrolidone, and extraction temperature is 66 ℃, and extracting pressure is 0.4MPa, and weight of solvent is 3.3 than (solvent/charging), isolates aromatic component and non-aromatic component; Gained aromatic component and solvent enter in the separation column 3 in the middle part, carry out fractionation by distillation, cut point is 120～180 ℃, fractionation pressure is 0.04～0.20MPa, bottom admission water lift, overhead fraction is a high-octane number component, the bottom side line extraction mouth aromatic component of attaching most importance to, and discharging is as circulating solvent at the bottom of the tower; The gained high-octane number component is all concocted with gasoline fraction; The gained non-aromatic component enters in the separation column 4 in the middle part, carries out fractionation by distillation, and cut point is 100～150 ℃, and pressure is 0.15～0.25MPa, and the cat head discharging is light non-aromatics, and discharging is a diesel component at the bottom of the tower; The gained diesel component is all concocted with diesel oil distillate; The light non-aromatics of gained is used as chemical industry light oil.
Comparative Examples 5
Paraffinic base heavy oil with 50% and 50% intermediate base heavy-oil catalytic raw material and recycle stock produce catalytic hydrocarbon under the LANET-35 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 110 ℃, the diesel oil temperature out is 190 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.11MPa, and tower bottom pressure is 0.12MPa, and fractionation obtains dry gas, liquefied gas, gasoline, diesel oil, heavy oil fraction etc.
As shown in Figure 2, cycloalkyl heavy oil fluid catalytic cracking raw material and recycle stock are produced catalytic hydrocarbon under the LANET-35 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 140 ℃, and the diesel oil temperature out is 220 ℃, and column bottom temperature is 370 ℃, tower top pressure is 0.1MPa, tower bottom pressure is 0.12Mpa, and the boiling range of described gasoline fraction 1 is controlled at 35～240 ℃, and the boiling range of diesel oil distillate is controlled at 240～385 ℃; Described gasoline fraction 1 pumps into separation column 2, carry out the fractionation second time, separation column 2 tower top temperatures are 80 ℃, the diesel oil temperature out is 240 ℃, column bottom temperature is 370 ℃, and tower top pressure is 0.1MPa, and tower bottom pressure is 0.12Mpa, it is 110 ℃～210 ℃ middle runnings that boiling range is isolated in described separation column 2 bottoms, and it is 35～110 ℃ gasoline fraction that boiling range is isolated at its top.Middle runnings pumps into the extraction plant tower and carries out solvent extraction and separation, solvent for use is 50% N-Methyl pyrrolidone and 50% Tetraglycol 99, and extraction temperature is 80 ℃, and extracting pressure is 0.4MPa, weight of solvent is 3.3 than (solvent/charging), isolates aromatic component and non-aromatic component; Gained aromatic component and solvent enter in the separation column 3 in the middle part, carry out fractionation by distillation, cut point is 120～180 ℃, fractionation pressure is 0.04～0.20MPa, bottom admission water lift, overhead fraction is a high-octane number component, the bottom side line extraction mouth aromatic component of attaching most importance to, and discharging is as circulating solvent at the bottom of the tower; Gained high-octane number component and gasoline fraction are mixed into 93# gasoline; The gained non-aromatic component enters in the separation column 4 in the middle part, carries out fractionation by distillation, and cut point is 100～135 ℃, and pressure is 0.15～0.25MPa, and the cat head discharging is light non-aromatics, and discharging is a diesel component at the bottom of the tower; Gained diesel component and diesel oil distillate are mixed into 5# diesel oil; The light non-aromatics of gained is used as chemical industry light oil.
Comparative Examples 6
With intermingled dregs ratio is that 60 paraffinic base heavy-oil catalytic raw material and recycle stock produce catalytic hydrocarbon under the LANET-35 catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 110 ℃, the diesel oil temperature out is 190 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.11MPa, and tower bottom pressure is 0.12MPa, and fractionation obtains dry gas, liquefied gas, gasoline, diesel oil, heavy oil fraction etc.
Embodiment 6
With intermingled dregs ratio is that 60 paraffinic base heavy-oil catalytic raw material and recycle stock produce catalytic hydrocarbon under the LCS catalyst action of Lanzhou catalyst plant production, the gained catalytic hydrocarbon adds separation column 1 and cuts fractionation, separation column 1 tower top temperature is 80 ℃, the diesel oil temperature out is 240 ℃, column bottom temperature is 370 ℃, tower top pressure is 0.1MPa, and tower bottom pressure is 0.12Mpa; Middle part at separation column 1 increases a side line extraction mouth, be used to cut middle runnings, side line extraction mouth temperature is 180 ℃, the boiling range scope of middle runnings is 140～240 ℃, and gained middle runnings pumps into extraction plant and carries out solvent extraction and separation, and solvent for use is five glycol, extraction temperature is 100 ℃, extracting pressure is 0.4MPa, and weight of solvent is 2.9 than (solvent/charging), isolates aromatic component and non-aromatic component; The gained aromatic component directly uses as premium-type gasoline; The gained non-aromatic component enters in the separation column 4 in the middle part, carries out fractionation by distillation, and cut point is 100～150 ℃, and pressure is 0.15～0.25MPa, and the cat head discharging is light non-aromatics, and discharging is a diesel component at the bottom of the tower; The gained diesel component is all concocted with diesel oil distillate; The light non-aromatics of gained is used as chemical industry light oil.
Yield and performance with Comparative Examples products obtained therefrom and embodiment products obtained therefrom is listed as follows below:
Table 1: Comparative Examples 1 compares with embodiment 1 product yield
| Product distributes | Comparative Examples 1 | | Variable quantity |
| Dry gas, m% | ????4.7 | ????4.7 | ????0 |
| Liquefied gas, m% | ????11.25 | ????11.25 | ????0 |
| Gasoline, m% | ????39.09 | ????29.38 | ????-9.71 |
| Diesel oil, m% | ????40.71 | ????46.53 | ????5.82 |
| Coke, m% | ????3.99 | ????3.99 | ????0 |
| Slurry oil, m% | ????0 | ????0 | ????0 |
| Chemical industry light oil, m% | ????0 | ????3.89 | ????3.89 |
| Loss, m% | ????0.3 | ????0.3 | ????0 |
Table 2: Comparative Examples 1 compares with embodiment 1 product performance
| Product distribute | Comparative Examples 1 | Embodiment 1 | Variable quantity |
| Aromaticity content in the gasoline, v% | ????23.1 | ????39.3 | ?????16.2 |
| Gasoline octane rating | ????90.2 | ????93.9 | ?????3.7 |
| The density of gasoline, kg/m 3 | ????718 | ????739 | ?????21 |
| Gasoline boiling range scope, ℃ | ????36～171 | ????36～204 | ?????- |
| Content of olefin in gasoline, v% | ????42.7 | ????37.5 | ?????-5.2 |
| Doing of gasoline, ℃ | ????171 | ????204 | ?????33 |
| Aromaticity content in the diesel oil, v% | ????48.2 | ????39 | ?????-9.2 |
| Diesel cetane-number | ????38 | ????43 | ?????5 |
| The density of diesel oil, kg/m 3 | ????847 | ????829 | ?????-18 |
| Diesel oil boiling range scope, ℃ | ????181～346 | ????167～346 | ?????- |
| Diesel-fuel flash point, ℃ | ????71 | ????57 | ?????-14 |
| Chemical industry light oil boiling range scope, ℃ | ????120～171 | ?????- | |
| Chemical industry light oil density, kg/m 3 | ????683 | ?????- | |
| Aromaticity content in the chemical industry light oil, v% | ????2.1 | ?????- | |
| Olefin(e) centent in the chemical industry light oil, v% | ????23 | ?????- |
Table 3: Comparative Examples 2 compares with embodiment 2 product yields
| Product distributes | Comparative Examples 2 | | Variable quantity |
| Dry gas, m% | ????6 | ????6 | ????0 |
| Liquefied gas, m% | ????9.5 | ????9.5 | ????0 |
| Gasoline, m% | ????41.5 | ????29.38 | ???-12.12 |
| Diesel oil, m% | ????23 | ????28.57 | ????5.57 |
| Coke, m% | ????9 | ????9 | ????0 |
| Slurry oil, m% | ????9 | ????9 | ????0 |
| Chemical industry light oil, m% | ????0 | ????6.55 | ????6.55 |
| The heavy aromatics component, m% | ????0 | ????0.8 | ????0.8 |
| Loss, m% | ????2 | ????0.3 | ????0 |
Table 4: Comparative Examples 2 compares with embodiment 2 product performance
| Product distributes | Comparative Examples 2 | Embodiment 2 | Variable quantity |
| Aromaticity content in the gasoline, v% | ????29 | ????41 | ????12 |
| Gasoline octane rating | ????91 | ????94.2 | ????3.2 |
| The density of gasoline, kg/m 3 | ????738 | ????751 | ????13 |
| Gasoline boiling range scope, ℃ | ??35～182 | ??36～204 | ????- |
| Content of olefin in gasoline, v% | ????58 | ????39.5 | ???-18.5 |
| Doing of gasoline, ℃ | ????182 | ????204 | ????33 |
| Aromaticity content in the diesel oil, v% | ????56 | ????40 | ???-16 |
| Diesel cetane-number | ????30 | ????38 | ????8 |
| The density of diesel oil, kg/m 3 | ????886 | ????854 | ???-18 |
| Diesel oil boiling range scope, ℃ | ??182～352 | ??165～346 | ????- |
| Diesel-fuel flash point, ℃ | ????75 | ????57 | ???-20 |
| Chemical industry light oil boiling range scope, ℃ | ??80～165 | ????- | |
| Chemical industry light oil density, kg/m 3 | ????667 | ????- | |
| Aromaticity content in the chemical industry light oil, v% | ????2.6 | ????- | |
| Olefin(e) centent in the chemical industry light oil, v% | ????42 | ????- | |
| Heavy aromatics component boiling range scope, ℃ | ??80～171 | ????- | |
| The heavy aromatics density of fraction, kg/m 3 | ????845 | ????- | |
| The aromaticity content of heavy aromatics component, m% | ????98.2 | ????- |
Table 5: Comparative Examples 3 compares with embodiment 3 product yields
| Product distributes | Comparative Examples 3 | | Variable quantity |
| Dry gas, m% | ????3.65 | ????3.65 | ????0 |
| Liquefied gas, m% | ????11.76 | ????11.76 | ????0 |
| Gasoline, m% | ????35.98 | ????28.07 | ???-7.91 |
| Diesel oil, m% | ????36.65 | ????44.56 | ????7.91 |
| Coke, m% | ????8.02 | ????8.02 | ????0 |
| Slurry oil, m% | ????3.75 | ????3.75 | ????0 |
| Loss, m% | ????0.24 | ????0.3 | ????0 |
Table 6: Comparative Examples 3 compares with embodiment 3 product performance
| Product distributes | Comparative Examples 3 | Embodiment 3 | Variable quantity |
| Aromaticity content in the gasoline, v% | ????21 | ????37 | ????16 |
| Gasoline octane rating | ????89 | ????92.1 | ????3.1 |
| The density of gasoline, kg/m 3 | ????723 | ????761 | ????13 |
| Gasoline boiling range scope, ℃ | ??35～203 | ??36～204 | ????- |
| Content of olefin in gasoline, v% | ????29 | ????36 | ????7 |
| Doing of gasoline, ℃ | ????203 | ????204 | ????1 |
| Aromaticity content in the diesel oil, v% | ????51 | ????40 | ????11 |
| Diesel cetane-number | ????29 | ????35 | ????6 |
| The density of diesel oil, kg/m 3 | ????887 | ????852 | ???-35 |
| Diesel oil boiling range scope, ℃ | ??203～349 | ??165～346 | ????- |
| Diesel-fuel flash point, ℃ | ????85 | ????56 | ???-29 |
Table 7: Comparative Examples 4 compares with embodiment 4 product yields
| Product distributes | Comparative Examples 4 | Embodiment 4 | Variable quantity |
| Dry gas, m% | ????4.21 | ????4.21 | ????0 |
| Liquefied gas, m% | ????12.61 | ????12.61 | ????0 |
| Gasoline, m% | ????47.04 | ????37.01 | ???-10.03 |
| Diesel oil, m% | ????22.82 | ????29.68 | ????6.86 |
| Coke, m% | ????7.42 | ????7.42 | ????0 |
| Slurry oil, m% | ????5.55 | ????5.55 | ????0 |
| Chemical industry light oil, m% | ????0 | ????3.17 | ????3.17 |
| Loss, m% | ????0.35 | ????0.35 | ????0 |
Table 8: Comparative Examples 4 compares with embodiment 4 product performance
| Product distributes | Comparative Examples 4 | Embodiment 4 | Variable quantity |
| Aromaticity content in the gasoline, v% | ????19 | ????38.5 | ????19.5 |
| Gasoline octane rating | ????89 | ????93 | ????4 |
| The density of gasoline, kg/m 3 | ????734 | ????756 | ????22 |
| Gasoline boiling range scope, ℃ | ??35～190 | ??36～204 | ????- |
| Content of olefin in gasoline, v% | ????33.33 | ????34.6 | ????1.27 |
| Doing of gasoline, ℃ | ????190 | ????204 | ????14 |
| Aromaticity content in the diesel oil, v% | ????52 | ????39 | ???-13 |
| Diesel cetane-number | ????32 | ????39 | ????7 |
| The density of diesel oil, kg/m 3 | ????887 | ????852 | ???-35 |
| Diesel oil boiling range scope, ℃ | ??203～363 | ??165～363 | ????- |
| Diesel-fuel flash point, ℃ | ????75 | ????56 | ???-19 |
| Chemical industry light oil boiling range scope, ℃ | ??100～165 | ????- | |
| Chemical industry light oil density, kg/m 3 | ????682 | ????- | |
| Aromaticity content in the chemical industry light oil, v% | ????2.9 | ????- | |
| Olefin(e) centent in the chemical industry light oil, v% | ????29 | ????- |
Table 9: Comparative Examples 5 compares with embodiment 5 product yields
| Product distributes | Comparative Examples 5 | | Variable quantity |
| Dry gas, m% | ????6.2 | ????6.2 | ????0 |
| Liquefied gas, m% | ????29.1 | ????29.1 | ????0 |
| Gasoline, m% | ????45.6 | ????33.6 | ???-12 |
| Diesel oil, m% | ????16.3 | ????21.6 | ????5.3 |
| Coke, m% | ????8.1 | ????8.1 | ????0 |
| Slurry oil, m% | ????0.2 | ????0.2 | ????0 |
| Chemical industry light oil, m% | ????0 | ????6.7 | ????6.7 |
| Loss, m% | ????0.5 | ????0.5 | ????0 |
Table 10: Comparative Examples 5 compares with embodiment 5 product performance
| Product distributes | Comparative Examples 5 | Embodiment 5 | Variable quantity |
| Aromaticity content in the gasoline, v% | ????33 | ????38.5 | ???19.5 |
| Gasoline octane rating | ????92.3 | ????97 | ???4.7 |
| The density of gasoline, kg/m 3 | ????741 | ????756 | ???22 |
| Gasoline boiling range scope, ℃ | ??35～192 | ??35～204 | ???- |
| Content of olefin in gasoline, v% | ????59 | ????51 | ??-8 |
| Doing of gasoline, ℃ | ????190 | ????204 | ???14 |
| Aromaticity content in the diesel oil, v% | ????52 | ????39 | ??-13 |
| Diesel cetane-number | ????32 | ????39 | ???7 |
| The density of diesel oil, kg/m 3 | ????887 | ????852 | ??-35 |
| Diesel oil boiling range scope, ℃ | ??203～363 | ??165～363 | ???- |
| Diesel-fuel flash point, ℃ | ????75 | ????56 | ??-19 |
| Chemical industry light oil boiling range scope, ℃ | ??100～165 | ???- | |
| Chemical industry light oil density, kg/m 3 | ????682 | ???- | |
| Aromaticity content in the chemical industry light oil, v% | ????2.9 | ???- | |
| Olefin(e) centent in the chemical industry light oil, v% | ????58 | ???- |
Table 11: Comparative Examples 6 compares with embodiment 6 product yields
| Product distributes | Comparative Examples 6 | Embodiment 6 | Variable quantity |
| Dry gas, m% | ????10.2 | ????10.2 | ????0 |
| Liquefied gas, m% | ????38.9 | ????38.9 | ????0 |
| Gasoline, m% | ????32.5 | ????25.1 | ???-7.4 |
| Diesel oil, m% | ????10.4 | ????14.3 | ????3.9 |
| Coke, m% | ????7.9 | ????7.9 | ????0 |
| Slurry oil, m% | ????0.2 | ????0.2 | ????0 |
| The heavy aromatics component, m% | ????0 | ????3.5 | ????3.5 |
| Loss, m% | ????0.3 | ????0.3 | ????0 |
Table 12: Comparative Examples 6 compares with embodiment 6 product performance
| Product distributes | Comparative Examples 6 | Embodiment 6 | Variable quantity |
| Aromaticity content in the gasoline, v% | ????36 | ????41.1 | ????5.1 |
| Gasoline octane rating | ????92.7 | ????93.9 | ????1.2 |
| The density of gasoline, kg/m 3 | ????748 | ????762 | ????14 |
| Gasoline boiling range scope, ℃ | ??35～195 | ??35～204 | ????- |
| Content of olefin in gasoline, v% | ????56 | ????58 | ???-2 |
| Doing of gasoline, ℃ | ????195 | ????204 | ????9 |
| Aromaticity content in the diesel oil, v% | ????56 | ????41 | ???-15 |
| Diesel cetane-number | ????26 | ????34 | ????8 |
| The density of diesel oil, kg/m 3 | ????891 | ????860 | ???-31 |
| Diesel oil boiling range scope, ℃ | ??203～356 | ??165～356 | ????- |
| Diesel-fuel flash point, ℃ | ????81 | ????56 | ???-25 |
| Heavy aromatics component boiling range scope, ℃ | ??204～240 | ????- | |
| The heavy aromatics density of fraction, kg/m3 | ????849 | ????- | |
| The aromaticity content of heavy aromatics component, m% | ????97.9 | ????- |
Aromaticity content in the diesel oil is tested with the GB11132-2002 method; Gasoline octane rating is tested with GB/T5487; The density of gasoline is tested with GB/T1884-1885; Gasoline boiling range scope is tested with GB/T6536; Content of olefin in gasoline is tested with the GB11132-2002 method; Aromaticity content in the diesel oil is tested with the GB11132-2002 method; Diesel cetane-number is tested with GB/T386; The density of diesel oil is tested with GB/T1884-1885; Diesel oil boiling range scope is tested with GB/T6536; Diesel-fuel flash point is tested with GB/T261; Chemical industry light oil boiling range scope is tested with GB/T6536; Chemical industry light oil density is tested with GB/T1884-1885; Aromaticity content in the chemical industry light oil is tested with the GB11132-2002 method; Olefin(e) centent in the chemical industry light oil is tested with the GB11132-2002 method.
Claims (9)
1, a kind of catalytic hydrocarbon reorganization treatment process is carried out fractionation with catalytic hydrocarbon by separation column (1), comprising fractionation gasoline fraction and diesel oil distillate; It is characterized in that: gasoline fraction and diesel oil distillate are reconfigured, between described gasoline fraction and diesel oil distillate, extract middle runnings out; Again extracting and separating is carried out in described middle runnings in solvent extraction plant, isolate aromatic component and non-aromatic component.
2, catalytic hydrocarbon reorganization treatment process according to claim 1 is characterized in that: fractionate out middle runnings by increasing one or more side line extraction mouths at described separation column (1) middle part; Described gasoline fractionation and diesel oil fractionation and intermediate fractionation are finished in described separation column (1); The boiling range of described gasoline fraction is controlled at 35～150 ℃, and the boiling range of described diesel oil distillate is controlled at 170～395 ℃, and the boiling range of described middle runnings is controlled at 70～250 ℃.
3, catalytic hydrocarbon reorganization treatment process according to claim 1 and 2, it is characterized in that: the tower top temperature of described separation column (1) is 65～130 ℃, the diesel oil temperature out is 170～250 ℃, described side line extraction mouth temperature is 120～240 ℃, and the column bottom temperature of described separation column (1) is 330～385 ℃; The tower top pressure of described separation column (1) is 0.15～0.28MPa, and the tower bottom pressure of described separation column (1) is 0.12～0.30MPa.
4, catalytic hydrocarbon reorganization treatment process according to claim 1, it is characterized in that: described fractionation is two step fractionation, the first step, elder generation's fractionation gasoline fraction and diesel oil distillate, the temperature of separation column (1) top and diesel oil extraction mouth is improved 10～50 ℃, the boiling range of described gasoline fraction is controlled at 35～250 ℃, and the boiling range of diesel oil distillate is controlled at 170～395 ℃; Described gasoline fraction pumps into separation column (2), carries out the fractionation second time, and described separation column (2) bottom side line extraction boiling range is 70～250 ℃ middle runnings, and it is 35～150 ℃ gasoline fraction that boiling range is isolated at its top
5, catalytic hydrocarbon reorganization treatment process according to claim 1, it is characterized in that: described fractionation is two step fractionation, the first step, elder generation's fractionation gasoline fraction and diesel oil distillate, the temperature of separation column (1) is reduced by 10～40 ℃, the boiling range of described gasoline fraction is controlled at 35～150 ℃, and the boiling range of diesel oil distillate (1) is controlled at 70～395 ℃; Described diesel oil distillate (1) pumps into separation column (5), carries out the fractionation second time, and described separation column (5) bottom side line extraction boiling range is 170～395 ℃ a diesel oil distillate, and it is 70～250 ℃ middle runnings that boiling range is isolated at its top.
6, according to the reorganization treatment process of claim 1 or 2 or 3 or 4 described catalytic hydrocarbon, it is characterized in that: described aromatic component is carried out fractionation in separation column (3), high octane gasoline component is isolated at described separation column (3) top, its underpart side line extraction heavy aromatics component; Gained high octane gasoline component and the blending of described gasoline fraction, gained heavy aromatics component and the blending of described diesel oil distillate, gained heavy aromatics component also can be used as stand-alone product and uses.
7, the reorganization treatment process of catalytic hydrocarbon according to claim 2 is characterized in that: 2 to 4 side line extraction mouths are drawn at described separation column (1) middle part, make middle runnings be divided into 2 to 4 logistics.
8, according to the reorganization treatment process of claim 1 or 2 or 3 or 4 described catalytic hydrocarbon, it is characterized in that: described aromatic component directly uses as premium-type gasoline.
9, according to the reorganization treatment process of claim 1 or 2 or 3 or 4 described catalytic hydrocarbon, it is characterized in that: described non-aromatic component carries out fractionation in separation column (4), described separation column (4) bottom side line extraction diesel component, and with the blending of itself and described diesel oil distillate, improve diesel-fuel cetane number, also can concoct out one or more low-coagulation diesel oils and non-low-coagulation diesel oil; Light non-aromatics is isolated at described separation column (4) top, and described light non-aromatics can be used as chemical industry light oil, also can concoct with described gasoline fraction.
Priority Applications (8)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031481817A CN1295302C (en) | 2003-07-04 | 2003-07-04 | Catalytic hydrocarbon reforming treatment method |
| CA2528631A CA2528631C (en) | 2003-07-04 | 2004-07-02 | A process for catalytic hydrocarbon recombination |
| PCT/CN2004/000723 WO2005003261A1 (en) | 2003-07-04 | 2004-07-02 | A method for recombining catalytic hydrocarbons |
| US10/563,351 US7867383B2 (en) | 2003-07-04 | 2004-07-02 | Method for recombining catalytic hydrocarbons |
| EP04738321A EP1650287B1 (en) | 2003-07-04 | 2004-07-02 | A method for recombining catalytic hydrocarbons |
| JP2006515639A JP4399454B2 (en) | 2003-07-04 | 2004-07-02 | Method for modifying catalytic cracking alkylate |
| EA200600180A EA008121B1 (en) | 2003-07-04 | 2004-07-02 | Method for processing catalysate |
| AT04738321T ATE551413T1 (en) | 2003-07-04 | 2004-07-02 | METHOD FOR RECOMBINATION OF CATALYTIC HYDROCARBONS |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB031481817A CN1295302C (en) | 2003-07-04 | 2003-07-04 | Catalytic hydrocarbon reforming treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1470607A true CN1470607A (en) | 2004-01-28 |
| CN1295302C CN1295302C (en) | 2007-01-17 |
Family
ID=34156219
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB031481817A Expired - Fee Related CN1295302C (en) | 2003-07-04 | 2003-07-04 | Catalytic hydrocarbon reforming treatment method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1295302C (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009067893A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| WO2009067885A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| CN101475833A (en) * | 2009-01-22 | 2009-07-08 | 北京金伟晖工程技术有限公司 | System and method for preparing high quality petrol by hydrogenation after component oil refining hydrocarbon recombination |
| CN101497807A (en) * | 2008-01-29 | 2009-08-05 | 丁冉峰 | System and method for preparing high quality petrol |
| WO2009094934A1 (en) * | 2008-01-29 | 2009-08-06 | Beijing Grand Golden-Bright Engineering & Technologies Co., Ltd | A system and a process for producing high quality gasoline |
| CN101429443B (en) * | 2007-11-09 | 2012-08-22 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN101429445B (en) * | 2007-11-09 | 2012-10-03 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN101429444B (en) * | 2007-11-09 | 2012-11-14 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN101429448B (en) * | 2007-11-09 | 2012-11-14 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN101429447B (en) * | 2007-11-09 | 2012-11-14 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| WO2012174860A1 (en) * | 2011-06-22 | 2012-12-27 | 北京金伟晖工程技术有限公司 | Device and method for low-cost production of low-sulphur, high-octane gasoline |
| CN101429442B (en) * | 2007-11-09 | 2013-02-06 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN111575045A (en) * | 2020-05-26 | 2020-08-25 | 中国海洋石油集团有限公司 | Method for reducing benzene and increasing aromatic hydrocarbon yield of desulfurized gasoline |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5310480A (en) * | 1991-10-31 | 1994-05-10 | Uop | Processes for the separation of aromatic hydrocarbons from a hydrocarbon mixture |
| FR2704232B1 (en) * | 1993-04-23 | 1995-06-16 | Inst Francais Du Petrole | PROCESS FOR IMPROVING THE QUALITIES OF A HYDROCARBON FILLER BY EXTRACTION AND HYDRODESULFURATION AND THE GAS OIL OBTAINED. |
| DE69917423T2 (en) * | 1998-08-21 | 2004-09-16 | Sasol Wax (South Africa) (Pty.) Ltd., Rosebank | METHOD FOR THE DISTILLATION OF FISCHER-TROPSCH PARAFFINS |
| CN1140606C (en) * | 2000-12-26 | 2004-03-03 | 中国石化集团洛阳石油化工工程公司 | Recovery method of diesel oil fraction in tower bottom heavy oil of atmospheric fractional tower |
-
2003
- 2003-07-04 CN CNB031481817A patent/CN1295302C/en not_active Expired - Fee Related
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101429448B (en) * | 2007-11-09 | 2012-11-14 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| WO2009067885A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| US8940154B2 (en) | 2007-11-09 | 2015-01-27 | Ranfeng Ding | System and process for producing high quality gasoline by catalytic hydrocarbon recombination |
| CN101429442B (en) * | 2007-11-09 | 2013-02-06 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| WO2009067893A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| CN101429443B (en) * | 2007-11-09 | 2012-08-22 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN101429447B (en) * | 2007-11-09 | 2012-11-14 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| CN101429445B (en) * | 2007-11-09 | 2012-10-03 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| EA017164B1 (en) * | 2007-11-09 | 2012-10-30 | Жаньфэн Дин | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| CN101429444B (en) * | 2007-11-09 | 2012-11-14 | 丁冉峰 | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline |
| WO2009094934A1 (en) * | 2008-01-29 | 2009-08-06 | Beijing Grand Golden-Bright Engineering & Technologies Co., Ltd | A system and a process for producing high quality gasoline |
| CN101497807A (en) * | 2008-01-29 | 2009-08-05 | 丁冉峰 | System and method for preparing high quality petrol |
| CN101497807B (en) * | 2008-01-29 | 2013-04-10 | 丁冉峰 | System and method for preparing high quality petrol |
| CN101475833B (en) * | 2009-01-22 | 2012-09-05 | 北京金伟晖工程技术有限公司 | Method for preparing high quality petrol by hydrogenation after component oil refining hydrocarbon recombination |
| CN101475833A (en) * | 2009-01-22 | 2009-07-08 | 北京金伟晖工程技术有限公司 | System and method for preparing high quality petrol by hydrogenation after component oil refining hydrocarbon recombination |
| WO2012174860A1 (en) * | 2011-06-22 | 2012-12-27 | 北京金伟晖工程技术有限公司 | Device and method for low-cost production of low-sulphur, high-octane gasoline |
| EA024334B1 (en) * | 2011-06-22 | 2016-09-30 | Бейджин Гранд Голден-Брайт Инджиниринг Энд Текнолоджиз Ко., Лтд. | Method and device for low-cost production of low-sulphur, high-octane gasoline |
| US9657245B2 (en) | 2011-06-22 | 2017-05-23 | Beijing Grand Golden-Bright Engineering & Technologies Co., Ltd. | Device of producing low-sulfur high-octane-number gasoline with low cost and method thereof |
| CN111575045A (en) * | 2020-05-26 | 2020-08-25 | 中国海洋石油集团有限公司 | Method for reducing benzene and increasing aromatic hydrocarbon yield of desulfurized gasoline |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1295302C (en) | 2007-01-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101045884B (en) | Process of producing clean diesel oil and low carbon olefin with residual oil and heavy fraction oil | |
| CN1295302C (en) | Catalytic hydrocarbon reforming treatment method | |
| CN101724457B (en) | Hydrogenation combined method for diesel oil | |
| CN1309802C (en) | Catalytic hydrocarbon recombinant treating method | |
| CN101067089A (en) | Shale oil producing process | |
| CN105647573A (en) | Method for producing light-weight aromatic hydrocarbons and clean fuel oil by moving bed hydrocracking | |
| CN1814703A (en) | Method for producing diesel or diesel composition using Fischer-Tropsch synthetic product | |
| CN1176189C (en) | Catalytic conversion method and apparatus for upgrading poor gasoline | |
| CN109988650B (en) | Hydrogenation modification and hydrofining combined method for poor diesel oil | |
| CN110257102A (en) | A kind of raw material classification rich in polycyclic aromatic hydrocarbon faces hydrogen pyrolysis and produces the production system and method for light aromatics | |
| CN1160746A (en) | Gasoline octane number-raising catalytic conversion method | |
| CN1699520A (en) | Process for preparing naphtha materials special for ethylene production device by using Fisher-Tropsch synthetic products | |
| CN1940030A (en) | Hydrogenation cracking method of high-output diesel oil from high-nitrogen content heavy raw material | |
| CN100532507C (en) | Catalytic cracking gasoline modifying method | |
| CN1277907C (en) | Recombinant processing method for naphtha | |
| CN100351346C (en) | Medium pressure hydrocracking process for preparing jet fuel | |
| CN109988643B (en) | Hydrogenation modification and hydrofining combined process for poor diesel oil | |
| CN115895722A (en) | System for preparing light aromatic hydrocarbon from heavy oil raw material | |
| CN105087047A (en) | Heavy oil catalytic cracking process for producing heavy and light arene products in productive mode | |
| CN105018138A (en) | Method and system for producing aromatic hydrocarbon, asphalt and high-octane gasoline through inferior crude oil | |
| CN109988625B (en) | Hydrofining and hydrocracking combined process | |
| CN1323058C (en) | Improved toluene disproportionation process | |
| CN1191334C (en) | Residual hydrogenation, catalytic cracking and diesel oil hydrogenation aromatics-removing combination method | |
| CN1151236C (en) | Catalytic conversion process of utilizing hydrogen donor component to reduce olefine content in gasoline | |
| CN1100121C (en) | Catalytic conversion method for reducing olefine, sulfur and nitrogen content in gasoline |
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 | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Effective date of registration: 20090305 Pledge (preservation): Pledge |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20140121 Granted publication date: 20070117 Pledgee: Zhongguancun Beijing technology financing Company limited by guarantee Pledgor: Ding Ranfeng|Beijing Golden Dragon Engineering Technology Co., Ltd. Registration number: 2009110000523 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Catalytic hydrocarbon reforming treatment method Effective date of registration: 20140121 Granted publication date: 20070117 Pledgee: Zhongguancun Beijing technology financing Company limited by guarantee Pledgor: Ding Ranfeng|Beijing Golden Dragon Engineering Technology Co., Ltd. Registration number: 2014990000056 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PM01 | Change of the registration of the contract for pledge of patent right |
Change date: 20140121 Registration number: 2009110000523 Pledgee after: Zhongguancun Beijing technology financing Company limited by guarantee Pledgee before: Zhongguancun Beijing science and technology Company limited by guarantee |
|
| PM01 | Change of the registration of the contract for pledge of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20070117 Termination date: 20190704 |