GB2134537A - For solvent deasphalting of petroleum - Google Patents
For solvent deasphalting of petroleum Download PDFInfo
- Publication number
- GB2134537A GB2134537A GB08401454A GB8401454A GB2134537A GB 2134537 A GB2134537 A GB 2134537A GB 08401454 A GB08401454 A GB 08401454A GB 8401454 A GB8401454 A GB 8401454A GB 2134537 A GB2134537 A GB 2134537A
- Authority
- GB
- United Kingdom
- Prior art keywords
- solvent
- mixture
- hydrocarbonaceous
- extruder
- water bath
- 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.)
- Withdrawn
Links
- 239000002904 solvent Substances 0.000 title claims abstract description 44
- 239000003208 petroleum Substances 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 claims abstract description 38
- 239000013557 residual solvent Substances 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000000638 solvent extraction Methods 0.000 claims abstract description 15
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims description 32
- 239000000203 mixture Substances 0.000 claims description 13
- 229930195733 hydrocarbon Natural products 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 6
- 239000004215 Carbon black (E152) Substances 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 4
- 125000004432 carbon atom Chemical group C* 0.000 claims description 2
- 125000001183 hydrocarbyl group Chemical group 0.000 claims 1
- 238000000605 extraction Methods 0.000 abstract description 4
- 238000011084 recovery Methods 0.000 description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical class CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 5
- 235000013849 propane Nutrition 0.000 description 3
- 235000013844 butane Nutrition 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000013467 fragmentation Methods 0.000 description 2
- 238000006062 fragmentation reaction Methods 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical class CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000011877 solvent mixture Substances 0.000 description 2
- 238000013022 venting Methods 0.000 description 2
- 241000220317 Rosa Species 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
After the major portion 15 of solvent has been removed by evaporative separation from the heavy phase asphaltene stream 9 from a petroleum solvent extraction process. The asphaltenes containing residual solvent is passed through a heated, vented extruder (35) and the volatilized solvent 53 is recovered and recycled to the extraction system. The asphaltene product can be extruded into a cold water bath (61), fragmented, dried, and collected. <IMAGE>
Description
SPECIFICATION
Process for solvent deasphalting of petroleum
This invention relates to a process for solvent deasphalting of a petroleum, and more particularly relates to the desolventizing of hydrocarbonaceous materials, containing residual solvent, which are produced in the solvent deasphalting of petroleum.
A number of processes exist which use solvent extraction of petroleum to separate hydrocarbonaceous materials, such as asphaltenes. Examples of such processes arethe Rose process and Demex process, which can be classified as supercritical solvent extraction process, and other conventional extraction processes, which have been described, for example in Hydrocarbon Processing magazine, September 1980, p.p. 196-199. Such processes extract useful oils from heavy petroleum material by rejecting hydrocarbonaceous materials, asphaltenes, using lightsolvents. Some residual solvent is contained in the heavy phase asphaltene stream, which solvent must be recovered for economical and environmental reasons.An existing method of solvent recovery uses a trayed stripping column, preceeded by a flash drum for the lightest solvents, which has a feed preheater and recirculation exchangerto hold the asphaltene at temperatures 100-500" F (38-66"C) above the ring and ball softening pointto facilitate stripping and handling. The stripped asphaltene is pumped by a gear or screw pump onto a water-cooled belt (flaker) to make a flaked productwhich can then be transported to a final user in bulk form. High temperatures, up to 500-550"F (260-288"C), are used for the asphaltene.
Examples of recentsuch solvent deasphalting processes and means for recovery solvent in such processes are described, for example, in U.S. patent nos. 4,273,644; 4,278,529; 4,279,379 and 4,315,815, which teach various methods for desolventizing of asphaltene-solvent heavy phase streams. Such methods use steam stripping ofthe heavy phase stream, and various methods are proprosed for preventing the carry-over offine asphaltenes in the recovered solvent. In U.S. patent no.4,315,815 there is described a specific steam stripping apparatus where the mixture isfed to a device which causes centrifugal motion and uses a vane structure to cause turbulence and separate fine particles of bituminous material from the vaporized solvent.
While the use of an extruding device has been known for use in various chemical processes, for example in U.S. patent no.3,874,090 wherein an extrusion dryer is used to dry polymeric material, using an adjustable restriction means to provide back pressure, or in U.S. patent no.4,206,713 where an extruder is used as a coal pump to plasticize coal particles or petroleum residuum, no process is known wherein asphaltenes formed from solvent deasphalting of petroleum have been desolventized using an extruding device.
The present invention aims to eliminate the need for a stripping tower and flaker so asto reduce energy and equipment costs, while recovering substantially all of the solventfrom an asphaltene material resulting from the solvent extraction of petroleum, by the use of an extruding device.
The present invention provides a process for solvent deasphalting of a petroleum wherein a heavy phase asphaltene stream containing hydrocarbonaceous material and a solvent is removed from a solvent extraction system, and subjected to evaporate separation to remove the major portion of the solvent in the said stream and produce a mixture of hydrocarbonaceous material containing residual solvent, comprising: (a) recovering residual solvent from the said mixture by passing the mixture through a vented extruder while heating the same to volatilize off the residual solvent; (b) collecting the volatilized solvent and recycling the same to the solvent extraction system; and (c) extruding a substantially solvent-free hydrocarbonaceous product from the extruder.
In the process according to the invention, residual solvent, in an asphaltene stream which contains hydrocarbonaceous material, the stream resulting as a heavy phase asphaltene stream from solvent deasphalting of a petroleum, which stream has been subjected to an evaporative separation of a major portion ofthe solvent, is recovered by passing the mixture of hydrocarbonaceous material and residual solventthrough a heated, vented extruderto volatize offthe residual solvent which is collected and recycled to the solvent extraction system, while extruding a substantially solvent-free hydrocarbonaceous product fro the extruder. The substantially solvent-free hydrocarbonaceous material is preferably extruded into a circulating cold water bath, dried, and separated from the water for subsequent use.The solvent may be suitably a hydrocarbon solvent selected from hydrocarbons having 3-5 carbon atoms.
The invention will be further described, by way of examples only, with referenceto the accompany drawing, which is a schematic illustration of a process for the recovery of residual solvent from an asphaltene stream produced in the solvent deasphalting of petroleum.
The present process provides a methodforthe desolventizing ofthe asphaltene stream that results from solvent extraction of petroleum.The process is usable in desolventizing asphaltenes produced in supercritical solvent extraction processes as well as in conventional extraction processes.
Referring nowto the drawing, a light hydrocarbon solventfrom line 1, and a petroleum residuum containing asphaltenesfrom line 3 and fed to an extraction vessel 5. The heavy oil, which is dissolved in solvent, is discharged from the vessel 5 for recovery through line 7. A heavy phase asphaltene stream is discharged from the vessel 5through line 9, the stream comprising hydrocarbonaceous material and solvent. The heavy phase aspha Itene stream is then passed through a valve 11 and into an evaporative separator 13, such as a flesh evaporator, where a major portion of the solvent in the stream is removed through line 15.
Solventthat is separated from the stream in the evaporate separator 13 passes through line 15to a condensor 17, and thence through a recovery system which comprises line 19, and a settler 21, in which any water is separated. Water is discharged from the settlerthrough line 23 for re-use, while the solvent is discharged through line 25 to a pump 27 and then through line 29 for use as recycle solvent in line 1.
The process described thus far is a conventional system for solvent extraction of a petroleum residuum, with use of flash evaporation to recover and recycle the major portion ofthe solvent carried by the heavy phase asphaltene stream back to the solvent extraction system.
The bottoms from the evaporative separator 13, which is a mixture of hydrocarbonaceous material containing residual solvent, is discharged through line 31 and through a valve 33 into a double screw vented extruder 35. The double screw vented extruder 35 is of conventional type wherein a material is advanced along a double barrel 39 having communication channels.Avent41 is provided along the barrel, with a low pressure zone provided, either exposed to atmos phericpressure or a vacuum, which provides venting of volatile material through the vent The twin screw extruder is needed due to the viscosity of the hydrocarbonaceous material being processed.Typical such double screw vented extruders are sold commercially, for example the Baker Perkins Reactor sold bythe Baker Perkins lnc.-Chemical Machine
Division, and other extruder manufacturers.
As schematically illustrated in the drawing, a double screw vented extruder 35 has a motor 37 for driving the doublescrews in the barrels 39 and a vent 41 intermediate the entry end 43 and discharge end 45 of the extruder. The vent is connected to a steam jet eductor47, provided with steam through line 49, to provide atmospheric pressure or subatmospheric pressure in the vent. Steam from a source, not shown, is charged to the extruder, and maintained separate from the material being processed,through lines 51 to provide indirect heating for the material, or other indirect heating means may be provided.
The temperature ofthe hydrocarbonaceous material-solvent mixture in the extruder should be maintained at a temperature of from about 200-370"F (93-188"C), at atmospheric pressure, so as to volatilize offthe solvent while passing the hydrocarbonaceous material through the extruder. In such a temperature range, the highest steam pressure required will be about 600 psig.
Asthemixtureofhydrocarbonaceous material containing residual solvent is charged to the double screw, heated, vented extruder at the entry end 43, the material is heated and volatilized residual solvent is discharged through the vent41,through line 53, and to steam eductor 47. The steam-solvent mixture formed in the eductorflows through line 55to join with solventfrom the evaporative separator 13, in line 15 and thenceto the condensor 17 and the recovery system previously described. A compressor C may be provided, in line 55, for use in systems using normally gaseous solvents such as propanes, butanes, or the like. The eductor could be replaced by a conventional vacuum pump.
A substantially solvent-free hydrocarbonaceous material, after venting of solvent through the vent 41, is then advanced along the extruder35 to the discharge end 45. Steam is provided, through line 57, to heata die plate 59through which the substantially solvent-free hydrocarbonaceous material is discharged. The substantially solvent4ree hydrocarbonaceous material is discharged through the die plate 59 into a chamber 61 containing a circulating cold water bath. The water quenching chills the substantially solvent-free hydrocarbonaceous material and facilitates a clean (non-smearing) fragmentation by a fly-knife 63, operated by a motor 65, or other fragmentation means.The fragmented, substantially solvent-free hydrocabonaceous material is carried by the circulating water bath through line 67to a dryer 69, preferably a centrifugal spin dryer,andthefrag- mented, substantially solvent-free hydrocarbonaceous material product is discharged through line 71 for use.
Waterfromthedryerpassesthrough line 73 to a sump 75. In the sump 75, any remaining solvent or hydrocarbon scum is removed and thewater is recycled through line77,which may contain afilter79, to a pump 81 and thence through line 53, which may contain a cooling means 85, back to the chamber 61 for re-use as a circulating cold water bath in cooling further extrudate.
In conventional processes, where the asphaltenes are fed to a flaker, the temperature of the asphaltene feed to the flaker is held attemperatures 100-150"F (38-66"C) above the ring and ball softening point, i.e.
upto 500-550"F (260-288"C). By use ofthe present process, wherein the operating temperatures are lower, about 200-370"F (93-188"C), the process heat efficiency will be increased by a minimum of about 100-185 BTU's per pound of asphaltene product for a pentaneto propane solvent extraction process equivalentto about 40,000-64,724 BTU per barrel of asphaltene product. Heat efficiencies are greater as the solvents become lighter,for example where butanes or propane are used.
The present process thus provides significant energy savings and also reduces the need for extensive air pollution control systems since the solvents will not be at the elevated temperature required in conventional processes.
Claims (10)
1. A process for solvent deasphalting of a pet roleumwherein a heavy phase asphaltene stream containing hydrocarbonaceous material and a solvent is removed from a solvent extraction system, and subjected to evaporative separation to remove the major portion ofthe solvent in the said stream and produce a mixture of hydrocarbonaceous material containing residual solvent, comprising: (a) recovering residual solvent from the said mixture by passing the mixture through a vented extruder while heating the same to volatilize off the residual solvent; (b) collecting the volatilized solvent and recycling the same to the solvent extraction system; and (c) extruding a substantially solvent-free hydrocarbo naceous product from the extruder.
2. A process as claimed in claim 1, wherein the extruder is vented to atmospheric or subatmospheric pressure.
3. A process as claimed in claim 1 or2, wherein the heating is effected so asto maintain a temperature of the mixture in the extruder of from about 200-370 F (93-188"C).
4. A process as claimed in any of claims 1 to 3, wherein the solvent is a hydrocarbon solvent selected from hydrocarbons having 3-5 carbon atoms.
5. A process as claimed in any of claims 1 to 4, wherein the substantially solvent-free hydrocarbonaceous product is extruded through a heated die into a cool water bath and fragmented therein.
6. A process as claimed in claim 5, wherein cooled, extruded, fragmented hydrocarbonaceous material from the water bath is dried and separated from the water.
7. A process as claimed in claim 6, wherein the water, following the said separation, is cooled and recycled to the said water bath.
8. A process as claimed in any of claims 1 to7, wherein the volatilized solvent is combined with solventfrom the evaporative separation priorto recycling to the solvent extraction system.
9. A process as claimed in claim 1,whichcom- prises:
recovering residual solvent from the said mixture of hydrocarbonaceous material and residual solvent by passing the mixture through a vented extruder, which is vented to atmospheric or subatmospheric pressure, while heating the same to maintain the temperature of the mixture therein at from about 200-3700F (93- 1 88"C), to volatilize offthe residual solvent;
collecting the volatilized solvent, combining the same with solventfromthe evaporative separation, and recycling the sametothesolventextraction system;
extruding a substantially solvent-free hydrocarbonaceous productthrough a heated die into a cool water bath; ;
fragmenting the said extruded substantially solvent-free hydrocarbonaceous product; and
separating the fragmented, substantially solventfree hydrocarbonaceous product from the water bath.
10. Aprocessaccordingtoclaim iforsolvent deasphalting of a petroleum, substantially as herein described with referenceto the accompanying
drawing.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US46334283A | 1983-02-03 | 1983-02-03 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB8401454D0 GB8401454D0 (en) | 1984-02-22 |
| GB2134537A true GB2134537A (en) | 1984-08-15 |
Family
ID=23839772
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB08401454A Withdrawn GB2134537A (en) | 1983-02-03 | 1984-01-19 | For solvent deasphalting of petroleum |
Country Status (9)
| Country | Link |
|---|---|
| JP (1) | JPS59176389A (en) |
| BE (1) | BE898840A (en) |
| DE (1) | DE3403484A1 (en) |
| ES (1) | ES8506339A1 (en) |
| FR (1) | FR2540509A1 (en) |
| GB (1) | GB2134537A (en) |
| GR (1) | GR81754B (en) |
| IT (1) | IT1173222B (en) |
| NL (1) | NL8400346A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0187947A1 (en) * | 1984-12-12 | 1986-07-23 | Lummus Crest, Inc. | Solvent for refining of residues |
| WO2019014751A1 (en) * | 2017-07-19 | 2019-01-24 | Meg Energy Corp. | Improved asphaltene conversion, separation, removal and transport preparation for heavy hydrocarbons |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7229065B2 (en) * | 2019-03-27 | 2023-02-27 | 住友重機械工業株式会社 | Injection molding machine |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB376756A (en) * | 1931-04-13 | 1932-07-13 | Walter Idris Jones | Improvements in or relating to the recovery of oil from oily sludges |
| GB1244773A (en) * | 1968-06-27 | 1971-09-02 | Exxon Research Engineering Co | Asphalt shearing process |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2495177B1 (en) * | 1980-11-28 | 1985-06-07 | Inst Francais Du Petrole | PROCESS FOR THE SOLVENT DEASPHALTATION OF HYDROCARBON RESIDUAL OILS |
-
1984
- 1984-01-19 GB GB08401454A patent/GB2134537A/en not_active Withdrawn
- 1984-02-01 DE DE3403484A patent/DE3403484A1/en not_active Ceased
- 1984-02-03 JP JP59017210A patent/JPS59176389A/en active Pending
- 1984-02-03 IT IT19445/84A patent/IT1173222B/en active
- 1984-02-03 GR GR73702A patent/GR81754B/el unknown
- 1984-02-03 FR FR8401698A patent/FR2540509A1/en not_active Withdrawn
- 1984-02-03 ES ES529461A patent/ES8506339A1/en not_active Expired
- 1984-02-03 NL NL8400346A patent/NL8400346A/en not_active Application Discontinuation
- 1984-02-03 BE BE0/212336A patent/BE898840A/en not_active IP Right Cessation
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB376756A (en) * | 1931-04-13 | 1932-07-13 | Walter Idris Jones | Improvements in or relating to the recovery of oil from oily sludges |
| GB1244773A (en) * | 1968-06-27 | 1971-09-02 | Exxon Research Engineering Co | Asphalt shearing process |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0187947A1 (en) * | 1984-12-12 | 1986-07-23 | Lummus Crest, Inc. | Solvent for refining of residues |
| WO2019014751A1 (en) * | 2017-07-19 | 2019-01-24 | Meg Energy Corp. | Improved asphaltene conversion, separation, removal and transport preparation for heavy hydrocarbons |
| US11001760B2 (en) | 2017-07-19 | 2021-05-11 | Suncor Energy Inc. | Asphaltene conversion, separation, removal and transport preparation for heavy hydrocarbons |
Also Published As
| Publication number | Publication date |
|---|---|
| ES529461A0 (en) | 1985-07-01 |
| FR2540509A1 (en) | 1984-08-10 |
| NL8400346A (en) | 1984-09-03 |
| DE3403484A1 (en) | 1984-08-09 |
| IT1173222B (en) | 1987-06-18 |
| GB8401454D0 (en) | 1984-02-22 |
| GR81754B (en) | 1984-12-12 |
| ES8506339A1 (en) | 1985-07-01 |
| IT8419445A0 (en) | 1984-02-03 |
| JPS59176389A (en) | 1984-10-05 |
| BE898840A (en) | 1984-05-30 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| WAP | Application withdrawn, taken to be withdrawn or refused ** after publication under section 16(1) |