CN1184842A - Extraction method for faulty wax oil solvent - Google Patents
Extraction method for faulty wax oil solvent Download PDFInfo
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- CN1184842A CN1184842A CN97121842A CN97121842A CN1184842A CN 1184842 A CN1184842 A CN 1184842A CN 97121842 A CN97121842 A CN 97121842A CN 97121842 A CN97121842 A CN 97121842A CN 1184842 A CN1184842 A CN 1184842A
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Abstract
In the invented extraction method for faulty paraffin oil we use the oil product with higher and wider boiling range and more saturated hydrocarbon oil product as back extractant in the extraction process. It can effectively extract the saturated hydrocarbon in the extract phase back to raffinate phase to cause the higher recovery of saturated hydrocarbon in the raffinate oil and lowering saturated hydrocarbon content in the extract oil, so as to improve the recovery of raffinate oil. At the same time the oil product time acting as the back extractant it itself is separated into raffinate phase and extract phase which are part of the products respectively. Therefore it needs no special recovery and recircle use, so that the load of solvent recovery system is decreased, the investment and operation costs are reduced.
Description
The invention belongs to oil refining and petrochemical industry, relate to the heavy oil deep processing, relate in particular to the improvement of faulty wax oil solvent extraction technology.
As everyone knows, faulty wax oil comprises wax oil and turning oil that hot-work such as delayed coking, thermally splitting, eureka produce, also comprises catalytic cracking recycle oil and slurry oil, and the mixture of the different ratios of straight-run gas oil inferior and above-mentioned oil product.Their common feature is to be rich in heavy arene, colloid and sulphur, nitrogen compound, is difficult to following process and handles.When they mix raw material do catalytic cracking, then because of containing a large amount of nitride or because of the heavy arene too high levels, its crackability is too poor, make light oil yield low, coke and dry gas yield height, oil stability is poor, therefore mixing limitedly, is not the ideal catalytically cracked material.When being used as hydrocracking raw material, also too high because of being rich in heavy arene and amount of nitrides, can only in straight-run gas oil, mix a spot of this class wax oil.Both just like this, also make the hydrocracking operational condition harsh more.As this class wax oil is carried out hydrotreatment, also, do reasons such as higher because of nitrogen and heavy arene too high levels in addition, intractable does not reach the ideal refining effect yet.Above-mentioned faulty wax oil is made with extra care by solvent extraction can be effectively with most heavy arenes, colloid and sulphur, nitrogen compound are extracted out, raffinating oil then is fine catalytic cracking or hydrocracking raw material, and the heavy arene content of extracting oil out is very high, is useful industrial chemicals.U.S. Pat 3654137 and US 3691061 are with after the wax oil extracting, raffinate oil and the oily raw material of doing catalytic cracking together of light extraction, and this device uses zeolite catalyst.Heavily extract the oily catalytic cracking unit that is used for non-zeolite catalysts out and make raw material.China patent CN 1042730A proposes to produce with technical combinations such as single solvent extraction and hydrogenation the technology of high-value product, 87107146.0 of CN utilize the solvent pairs extraction technique, compare with single solvent technology, its remarkable advantage is, it can make in the faulty wax oil cracking performance, and the rate of recovery of stable hydrocarbon in raffinating oil is higher preferably, thereby the yield of raffinating oil is higher, can obtain more catalytic cracking or hydrocracking raw material.Make the saturated hydrocarbon content of extracting oil out lower simultaneously, help its utilization.Extractive second solvent of solvent pairs is called the back suction agent in above-mentioned patent, is to be 90～120 ℃ solvent oil with boiling range.Though the solvent pairs extracting has significant advantage, more reasonable economically, after the agent of introducing back suction, increased the equipment and the operational load of recovery system, all corresponding increase of plant investment, material consumption, energy consumption.
The objective of the invention is to develop a kind of faulty wax oil solvent extraction technology, make above-mentioned faulty wax oil behind solvent extraction, raffinating oil becomes the high quality raw material of catalytic cracking or hydrocracking, and extracting oil out becomes and be rich in heavy arene, the good industrial chemicals of application prospect.
Technological core of the present invention is that the back suction agent boiling range that proposes at CN 87107146.0 is lower and the shortcoming brought is rich in stable hydrocarbon and develop to use, and higher, the wideer oil product of boiling range is done the back suction agent of extractive process.Proposed a kind of method for extracting of faulty wax oil solvent thus, idiographic flow is referring to accompanying drawing 1.Faulty wax oil 1 advances extraction tower 3, and the faulty wax oil initial boiling point should be controlled at＞and 300 ℃, best more than 320 ℃.Main solvent 5 is advanced on extraction tower top, and the bottom advances back suction agent 2 or back suction agent 2 is mixed into extraction tower with raw material.Raffinate 4 removes solvent from the top outflow through stripping tower 7 and goes out to raffinate oil 9 from tower bottom flow, and solvent advances separating tank 16 from cat head through condensation, recycles after settlement separate.Through the laggard stripping tower 13 of flashing tower 10 flash distillations, behind stripping, go out to extract oil 15 out from the effusive Extract in 3 ends of tower from tower 13 underflows, from the effusive aldehyde steam in tower 10,13 tops through the laggard separating tank 16 of condensation.The aldehyde sewage 17 that contains in jars 16 returns jars 16 after containing the aldehyde vapor condensation by bottom effluent sewerage, top behind stripping tower 19 strippings.In the further back suction of the stable hydrocarbon in the extract phase, itself is divided into two parts and discharges with a part of taking out surplus and extract phase and become product in tower 3 in the back suction agent.The faulty wax oil of above-mentioned indication comprises the mixture of the different ratios of wax oil that delayed coking, fluid coking, thermally splitting, eureka hot procedure produce and turning oil, catalytic cracking recycle oil and slurry oil, straight-run gas oil inferior and above-mentioned three kinds of oil products.Described main solvent is wet furfural, phenol, the N-Methyl pyrrolidone of dried furfural, moisture 3～5m%, and the Extract of furfural in the refined course of lubricating oil or phenol.The present invention adopts higher, the wideer oil product that is rich in stable hydrocarbon of a kind of boiling range as the back suction solvent, this back suction solvent is in separation and purification extracting product, also be separated into two accompany raffinate and Extracts and discharge, become the part of useful products, and do not need special recycling.Described back suction solvent is 200～550 ℃ of boiling ranges, the best is 350～500 ℃, the oil product of saturated hydrocarbon content 〉=50m%, it comprises the raffinating oil etc. of solvent extraction of straight run oil or thermally splitting wax oil and turning oil, catalytic cracking recycle oil and slurry oil, wax tailings and turning oil.The operational condition of extraction tower is as follows during extracting: solvent ratio is: main solvent: raw material: back suction solvent=0.3～2.0: 1.0: 0.2～1.0 (weights), the optimum solvent ratio is 0.5～1.2: 1.0: 0.2～0.6 (weight).The extracting tower top temperature is 60～100 ℃, is 40～60 ℃ at the bottom of the tower.
The effect that the present invention reached be the back suction agent in extractive process, itself also is separated into the part of taking out surplus phase and extract phase and becoming product, does not need it is carried out special recycle and reuse.Therefore the present invention has reduced the load of the solvent recovering system of device, as after using back suction agent of the present invention, compares with the back suction agent of CN 87107146.0, and the vapour phase load of solvent recovering system reduces about 25～30%, and heat of phase transformation reduces about 20～25%.So obviously reduced investment and process cost, approximately both respectively save 15～25%.Faulty wax oil solvent extraction technology of the present invention is with the difference of feedstock property, and the yield of raffinating oil can reach 45～85% (weights), and the denitrification percent of raffinating oil is 70～85%, and desulfurization degree is 40～60%, takes off aromatic hydrocarbons rate 30～80%, the matter of coming unstuck rate 30～60%.Compare with raw material, the stable hydrocarbon and the hydrogen richness of raffinating oil obviously increase, and sulphur, nitrogen content obviously descend, and are good catalytic cracking of cracking performance or hydrocracking raw material.The stable hydrocarbon rate of recovery of raffinating oil is more than 95%, and the aromatic hydrocarbons+colloid of extracting oil out is greater than 95%, and saturated hydrocarbon content is to use wide industrial chemicals less than 5%.
Accompanying drawing and explanation thereof
Accompanying drawing 1 is the inventive method schematic flow sheet
1---raw material 10---flashing tower
2---back suction agent 12---Extract
3---extraction tower 13---stripping tower
4---raffinates 15---are extracted oil out
5---main solvent 16---separating tank
6---Extracts 17---contain aldehyde sewage
7---stripping tower 18---aldehyde liquid
8,11,14---main solvent 19---sewage stripping tower
9---raffinating oil 20---sewage
Embodiment 1
Certain wax tailings, its main character is: density (20 ℃) 0.9103g/cm
3, sulphur content 0.27% (weight), nitrogen content 0.65% (weight), aromatic hydrocarbons 32.3% (weight), colloid 9.2% (weight).
Use the test-results of the technology of the present invention and list in table-1, for more also listing the result of single solvent extraction and solvent pairs extracting (the back suction agent is 90～120 ℃).As can be seen, the technology of the present invention saturated hydrocarbon content in raffinate oil the yield stable hydrocarbon rate of recovery and extraction oil all has par with the solvent pairs extracting.But investment and process cost corresponding low 15～25%.Compare with single solvent extraction, the yield of then raffinating oil, the stable hydrocarbon rate of recovery is higher, and saturated hydrocarbon content is lower in the extraction oil.
Table-1
The single solvent extraction main solvent of project solvent pairs extracting of the present invention furfural, (5% water) furfural, (5% water) furfural, (doing) back suction agent boiling range ℃ 285～540 90～120/solvent ratio, (main: former: anti-), (weight) raffinated oil in 0.8: 1.0: 0.4 0.8: 1.0: 0.3 0.8: 1: yield m% 81.8 77.4 72.2
Character: sulphur μ g/g 1458
Nitrogen μ g/g 1368
Aromatic hydrocarbons m% 21.3
Stable hydrocarbon rate of recovery m% 96.8 97.3 90.8 investment and process cost relatively 1.0 1.15～1.25 1.0
Embodiment 2
Certain its main character of catalysis recycle stock is: density (20 ℃) 0.9906g/cm
3, sulphur content 3750 μ g/g, nitrogen content 3793 μ g/g, aromaticity content 58.6m%.
Use the experiment condition of the technology of the present invention and the results are shown in table-2.Also list simultaneously single solvent extraction and the extractive result of solvent pairs.Can draw same conclusions with embodiment 1 by table, show superiority of the present invention.
Table-2
The dried furfural back suction of the single dried furfural of the dried furfural of solvent extraction main solvent of project solvent pairs extracting of the present invention agent boiling range ℃ 330-510 90-120/solvent ratio (main: former: anti-) (weight) was raffinated oil in 0.5: 1: 0.3 0.5: 1: 0.3 0.5: 1: yield m% 55.4 47.2 41.5
Character: sulphur μ g/g 840
Nitrogen μ g/g 540
Aromatic hydrocarbons m% 11.2
Stable hydrocarbon rate of recovery m% 96.4 97.1 89.2 investments and process cost be 1.0 1.15-1.25 1.0 relatively
Claims (5)
1. extraction method for faulty wax oil solvent, it is characterized in that faulty wax oil 1 advances extraction tower 3, the faulty wax oil initial boiling point should be controlled at＞and 300 ℃, best more than 320 ℃, main solvent 5 is advanced on extraction tower top, the bottom advances back suction agent 2 or back suction agent 2 is mixed into extraction tower with raw material, raffinate 4 removes solvent from the top outflow through stripping tower 7 and goes out to raffinate oil 9 from tower bottom flow, solvent advances separating tank 16 from cat head through condensation, after settlement separate, recycle, from the effusive Extract in 3 ends of tower through the laggard stripping tower 13 of flashing tower 10 flash distillations, behind stripping, go out to extract out oil 15 from tower 13 underflows, from tower 10, the effusive aldehyde steam in 13 tops is through the laggard separating tank 16 of condensation, in jars 16 contain aldehyde sewage 17 behind stripping tower 19 strippings by the bottom effluent sewerage, jar 16 is returned after containing the aldehyde vapor condensation in the top, in the further back suction of the stable hydrocarbon in the extract phase, itself is divided into two parts and discharges with a part of taking out surplus and extract phase and become product in tower 3 in the back suction agent.
2. extraction method for faulty wax oil solvent according to claim 1, the faulty wax oil that it is characterized in that indication comprise the mixture of the different ratios of wax oil that delayed coking, fluid coking, thermally splitting, eureka hot procedure produce and turning oil, catalytic cracking recycle oil and slurry oil, straight-run gas oil inferior and above-mentioned three kinds of oil products.
3. extraction method for faulty wax oil solvent according to claim 1 is characterized in that described main solvent is wet furfural, phenol, the N-Methyl pyrrolidone of dried furfural, moisture 3～5m%, and the Extract of furfural in the refined course of lubricating oil or phenol.
4. extraction method for faulty wax oil solvent according to claim 1, it is characterized in that described back suction solvent is 200～550 ℃ of boiling ranges, the best is 350～500 ℃, the oil product of saturated hydrocarbon content 〉=50m%, it comprises the raffinating oil of solvent extraction of straight run oil or thermally splitting wax oil and turning oil, catalytic cracking recycle oil and slurry oil, wax tailings and turning oil.
5. extraction method for faulty wax oil solvent according to claim 1, the operational condition of extraction tower is as follows when it is characterized in that extracting: solvent ratio is: main solvent: raw material: back suction solvent=0.3～2.0: 1.0: 0.2～1.0 (weights), the optimum solvent ratio is 0.5～1.2: 1.0: 0.2～0.6 (weight), the extracting tower top temperature is 60～100 ℃, is 40～60 ℃ at the bottom of the tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97121842A CN1061366C (en) | 1997-12-08 | 1997-12-08 | Extraction method for faulty wax oil solvent |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97121842A CN1061366C (en) | 1997-12-08 | 1997-12-08 | Extraction method for faulty wax oil solvent |
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| Publication Number | Publication Date |
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| CN1184842A true CN1184842A (en) | 1998-06-17 |
| CN1061366C CN1061366C (en) | 2001-01-31 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN97121842A Expired - Fee Related CN1061366C (en) | 1997-12-08 | 1997-12-08 | Extraction method for faulty wax oil solvent |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102453503A (en) * | 2010-10-25 | 2012-05-16 | 中国石油化工股份有限公司 | Method for extracting and separating aromatic hydrocarbon and saturated hydrocarbon in catalytic cracking slurry oil |
| CN102676214A (en) * | 2011-03-08 | 2012-09-19 | 中国石油天然气股份有限公司 | Solvent refining method and equipment for producing environment-friendly rubber filling oil |
| CN104593052A (en) * | 2015-01-19 | 2015-05-06 | 中国石油天然气股份有限公司 | Solvent refining equipment and method for inferior coker gas oil |
| CN112980504A (en) * | 2019-12-17 | 2021-06-18 | 中国石油大学(北京) | Process and device for preparing oil product by mixing oil slurry, recycle oil and coking wax oil |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4304660A (en) * | 1980-04-14 | 1981-12-08 | Texaco Inc. | Manufacture of refrigeration oils |
| CN1003601B (en) * | 1987-10-30 | 1989-03-15 | 中国石油化工总公司洛阳石油化工工程公司 | Catalytic cracking-catalytic heavy oil aromatic extraction combined process |
| CN1022844C (en) * | 1989-09-11 | 1993-11-24 | 齐鲁石油化工公司研究院 | Method for producing high-value product by using wax oil |
-
1997
- 1997-12-08 CN CN97121842A patent/CN1061366C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102453503A (en) * | 2010-10-25 | 2012-05-16 | 中国石油化工股份有限公司 | Method for extracting and separating aromatic hydrocarbon and saturated hydrocarbon in catalytic cracking slurry oil |
| CN102453503B (en) * | 2010-10-25 | 2014-04-30 | 中国石油化工股份有限公司 | Method for extracting and separating aromatic hydrocarbon and saturated hydrocarbon in catalytic cracking slurry oil |
| CN102676214A (en) * | 2011-03-08 | 2012-09-19 | 中国石油天然气股份有限公司 | Solvent refining method and equipment for producing environment-friendly rubber filling oil |
| CN102676214B (en) * | 2011-03-08 | 2014-06-04 | 中国石油天然气股份有限公司 | Solvent refining method and equipment for producing environment-friendly rubber filling oil |
| CN104593052A (en) * | 2015-01-19 | 2015-05-06 | 中国石油天然气股份有限公司 | Solvent refining equipment and method for inferior coker gas oil |
| CN112980504A (en) * | 2019-12-17 | 2021-06-18 | 中国石油大学(北京) | Process and device for preparing oil product by mixing oil slurry, recycle oil and coking wax oil |
| CN112980504B (en) * | 2019-12-17 | 2022-12-30 | 中国石油大学(北京) | Process and device for preparing oil product by mixing oil slurry, recycle oil and coking wax oil |
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| CN1061366C (en) | 2001-01-31 |
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