WO2002102938A1 - Method of separating particles from a hydrocarbon composition - Google Patents
Method of separating particles from a hydrocarbon composition Download PDFInfo
- Publication number
- WO2002102938A1 WO2002102938A1 PCT/ZA2002/000101 ZA0200101W WO02102938A1 WO 2002102938 A1 WO2002102938 A1 WO 2002102938A1 ZA 0200101 W ZA0200101 W ZA 0200101W WO 02102938 A1 WO02102938 A1 WO 02102938A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- solvent
- particulate matter
- water
- crude tar
- solid particulate
- Prior art date
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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
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/04—Dewatering or demulsification of hydrocarbon oils with chemical means
Definitions
- This invention relates to a method of separating particles from a hydrocarbon composition prior to refining of said composition and, more specifically, to the separation of coal and ash particles from a crude tar feed derived from the gasification of coal.
- hydrocarbon streams are produced which are processed further to obtain a range of chemical products.
- One such hydrocarbon stream is a so-called crude tar feed stream that is further refined to produce tar.
- Said crude tar feed stream contains solid particles that are typically fine coal particles and/ or ash and which must be separated from the tar feed prior to refining.
- the inventor is aware of decanting and filtration methods used in the industry to separate the unwanted solid particulate matter from the crude tar feed prior to refining.
- the inventor therefore believes, that a need exists for a cost-effective method of separating a substantial amount of solid particulate matter from a crude tar feed as described above.
- a method of reducing solid particulate matter content of a crude tar feed which crude tar feed includes a hydrocarbon fluid fraction, a water fraction, and a solid particulate matter fraction which is at least partially coated with the hydrocarbon fluid fraction, the method including at least the steps of:- introducing a solvent into the crude tar feed; and removing from the solid particulate matter at least a portion of the hydrocarbon fluid fraction that coats the solid particulate matter while decreasing the density of the crude tar feed to well below the density of water and of the solid particulate matter in the crude tar feed.
- a typical crude tar feed when analysed according to ASTM D1160 has the following boiling point analysis as shown in table 1.
- the method may further include the step of allowing the resulting mixture to settle into a water phase and a hydrocarbon phase or tar phase for a predetermined period of time and to allow at least a fraction of the solid particulate matter to migrate from the hydrocarbon phase into the water phase.
- the migration mechanism for the solid particulate matter from the hydrocarbon phase into the water phase may be gravity settling.
- the method may include the use of a wetting agent as a settling aid for settling fine particles from out of the hydrocarbon phase into the water phase.
- the method may include the use of a de-emulsifying agent as a settling aid for settling fine particles from out of the hydrocarbon phase into the water phase.
- the method may further include the step of separating the water phase and the solvent from the hydrocarbon phase by any suitable separation process.
- the water and solvent phase may be separated from the hydrocarbon phase by centrifugation or distillation.
- the hydrocarbon fluid fraction that coats the solid particulate matter in the crude tar feed may be a tar fraction including asphaltenes.
- the solvent may be any solvent capable of washing off matter that coats the solid particulate matter so as to free the solid particulate matter for migration from the hydrocarbon phase into the water phase.
- the solvent may be a solvent rich in benzene but may alternatively be a solvent rich in toluene, xylene, paraffins, pyridine, quinoline or the like.
- a benzene rich solvent may typically include about 40 mass percent benzene and alkyl benzenes, about 27 mass percent xylenes and toluene, about 17 mass percent alkenes and dienes, about 10 mass percent alkanes and about 3 mass percent alcohols and carbonyls, the remainder of the solvent being made up by miscellaneous compounds.
- the solvent may have about 39 mass% benzene, about 21.5 mass% toluene, and about 4 mass% xylene.
- the solvent may have an analysis approaching that appearing in table 2 below.
- the solvent may be RectisolTM Naphtha solvent available from SasolTM in South
- the mass ratio of crude tar feed to solvent on addition of the solvent may be between 1 :5 and 3 :2 and is typically about 2:5, or even 1:1.
- the method may include adding water to the crude tar feed before, during or after the addition of the solvent, but typically after addition of the solvent.
- the amount of water added is a function of the amount of solid particulate matter particles contained in the crude tar feed and is typically 0,4 volume percent or more of the crude tar feed.
- the crude tar feed, solvent and water may be fed to a settling tank to allow separation of the hydrocarbon phase and water phase from the mixture.
- the solvent and crude tar feed may be mixed prior to the addition of water to allow the solvent to access the matter coating the solid particulate matter particles in the crude tar feed.
- the feed line to the settling tank may include a valve, mixing orifice or any other suitable mixing device to achieve high shear mixing in a fluid flowing into the settling tank.
- the fluid flowing into the settling tank may be a crude tar feed or a crude tar feed - water mixture and is typically a crude tar feed-water-solvent mixture.
- the temperature and pressure in the settling tank may be such that the solvent remains a liquid, i.e. below the boiling point of the solvent.
- the pressure in the settling tank may be between atmospheric and 14 bar and is typically about 1-3 bar.
- the temperature in the settling tank may be between ambient and 150°C and is typically about 30-40°C.
- the settling tank may be a conventional desalination tank known in the art or may be any other suitable settling tank. Typically, however, the settling tank is a conical bottom type tank.
- the crude tar feed, water and solvent mixture may be allowed to separate in the settling tank for between 15 and 120 minutes, preferably between 30 and 90 minutes and typically for about 45 minutes.
- Migration of the solid particulate matter from the hydrocarbon phase to the water phase may be improved by ionisation of the solid particulate matter.
- Methods such as electrostatic precipitation may be used to improve settling of the solid particulate matter into the water phase.
- the water phase that now contains the solid particulate matter that has migrated out of the hydrocarbon phase may be pumped out of the settling tank.
- the remaining hydrocarbon phase may then be subjected to trim filtration to obtain the desired solid particulate matter content which is typically about 0,02 percent by mass when measured by the ashing method or loss on ignition method.
- hydrocarbon phase may be fed to an evaporator for distillation where the solvent is distilled from the tar fraction after which the solvent may be recycled.
- a method analogous to the method as described above may be used in other applications where solid particulate matter needs to be separated from a viscous liquid coating said matter, for example, the method may be used to separating catalyst particles from a fluid catalytic cracking slurry or for separating solid particulate matter from an oily mixture.
- Figures 1, and 4 show schematic flow diagrams of a method of separating particulate matter from a crude tar feed that includes water and particulate matter in accordance with the present invention
- Figures 2 and 3 show graphical representations of Tables 3 and 4 below.
- reference numeral 10 generally indicates a process wherein a method of separating particulate matter from a crude tar feed which includes water and particulate matter in accordance with the present invention is utilised.
- the method of separating particulate matter (not shown) from a crude tar feed 12 which includes water and particulate matter includes adding a solvent stream 14 to the crude tar feed 12 for removing matter that coats the solid particulate matter particles with a fluid constituent of the crude tar feed 12 by dissolving at least a portion of it and for decreasing the density of the crude tar feed 12 to well below the density of water and of the solid particulate matter in the crude tar feed 12.
- the crude tar feed 12 typically contains about 10 percent by mass water.
- the size distribution of particulate matter in the crude tar feed 12 is typically such that 50 percent thereof is larger than 50 micron and 10 percent thereof is less than 10 micron.
- the matter that coats the particles or particulate matter in the crude tar feed 12 is typically a tar fraction including asphaltenes.
- the solvent may be any solvent capable of washing off matter which coats the solid particulate matter so as to free the solid particulate matter for migration from the hydrocarbon phase into the water phase.
- the solvent 14 is a solvent rich in benzene and typically includes about 40 mass percent benzene and alkyl benzenes, about 27 mass percent xylenes and toluene, about 17 mass percent alkenes and dienes, about 10 mass percent alkanes and about 3 mass percent alcohols and carbonyls, the remainder of the solvent being made up by miscellaneous compounds.
- the mass ratio of crude tar feed 12 to solvent 14 on addition of the solvent 14 is typically about 1:1.
- the solvent 14 and crude tar feed 12 are allowed to mix thoroughly to allow the solvent 14 to access the matter coating the solid particulate matter particles in the crude tar feed 12.
- a water stream 16 is also added to the crude tar feed 12.
- the amount of water 16 added is typically a function of the amount of solid particulate particles in the crude tar feed.
- a wetting agent or demulsifier (chemical) is added to the water stream 16 to assist the solid particulate settling in the settling tank.
- An additional water stream 22 is provided to provide additional water if necessary.
- the crude tar feed, solvent and water mixture 18 is fed to a settling tank 20 to allow separation of a hydrocarbon phase 24 and a water phase 26 from the mixture 18.
- the feed line to the settling tank 20 includes a mixing device 28 to create high shear mixing in the mixture 18.
- the mixture 18 is allowed to settle for about 45 minutes to allow the solid particulate matter to migrate from the hydrocarbon phase 24 into the water phase 26.
- the settling tank 20 is a conventional desalination tank known in the art or conical bottom type for ease of solids removal..
- the temperature and pressure in the settling tank 20 is such that the solvent 14 remains a liquid, i.e. below the boiling point of the solvent 14.
- the pressure in the settling tank 20 is typically about 1-3 bar and the temperature in the settling tank 20 is typically about 30-40°C.
- the water phase 26 that now contains the solid particulate matter that has migrated out of the hydrocarbon phase 24 is pumped out of the settling tank 20.Stream 26 is then subjected to filtration to remove the solids from the water. Residue water is returned to the process.
- solvent and water mixture 18 is fed to a settling tank 20 to allow separation of a hydrocarbon phase 24 and a water phase 26 from the mixture 18, the mixture is fed to a centrifuge 50 which serves both as a contactor for the components of mixture 18 as well as to separate the solids from the water phase (26 in Figure 1) into which the particles have migrated and the hydrocarbon phase 24 is treated similarly to that in Figure 1 as is described below.
- the hydrocarbon phase 24 is fed to an evaporator 30 for distillation where the solvent 14 is distilled from the tar fraction 34 after which the solvent 14 is recycled.
- the hydrocarbon phase 24 is subjected to trim filtration in filtration unit 32 prior to distillation.
- the tar fraction 34 thus obtained typically contains about 0,02 mass percent solid particulate matter.
- the solvent used during all examples typically had the following composition in mass percent:
- a sample of crude tar feed was obtained from a tar feed tank and was homogenized by stirring continuously before use.
- the ash content of crude tar sampled was 2,115 mass percent.
- each respective crucible was ignited and allowed to burn in order to remove the carbonaceous material.
- the residual material obtained in each crucible was ashed at 600 °C.
- Table 4 Settling time v solids content of a 40/60 (m/m) tar-solvent mixture with neat crude tar feed as reference
- a mixture of 60 g solvent and 40 g of crude tar was prepared in a glass bottle.
- the bottle was stoppered and the content was shaken-up for 2 minutes.
- An amount of tap water (50 cm 3 ) was added to the contents in the bottle and allowed to separate for 30 minutes.
- the water phase with the solid material was filtered through a Whatman 41 filter paper.
- the benzene-washed solid material was dried in an oven at 105 °C.
- the dried solid material was then ashed at 900 °C and the remaining ash fused with LiBO 2 at 900 °C.
- the flux was dissolved in hydrochloric acid (1:1), diluted to a known volume and the metal content determined using ICP-AES.
- Table 5 Typical Composition of the solid material settled out from the crude tar feed
- the solids content (measured as ash content) of the crude tar feed as sampled was 2,115 mass percent.
- the solids remaining in suspension reduced to 1,974 mass percent for a settling time of 15 minutes and to 1 ,377 mass percent after a settling time of 60 minutes.
- Table 3 and Figure 2 show that for a settling time of 1 hour, little variation in the solids content of the tar fractions (measured as ash content) is obtained for the tar-solvent mixtures, containing 50 mass percent or less tar.
- Adequate separation of the solid material from the tar should be obtained for any tar-solvent mixture containing less than or equal to 50 mass percent tar.
- a tar-solvent mixture containing 50 percent tar relates to a solids content of 0,059 mass %
- a tar-solvent mixture containing 40 percent tar relates to a solids content of 0,057 mass %
- a tar-solvent mixture containing 20 percent tar relates to a solids content of 0,052 mass%
- Table 4 and Figure 3 show that for a chosen optimum ratio of 40% tar and 60% solvent settling of the solid material is obtained within 15 minutes, after shaking the mixture for 2 minutes.
- the viscosity and density of these mixtures allow for the settling of the denser solid material into the water phase.
- An additional filtration of the tar-solvent mixture will reduce the ash content to within the desired limit of less than or equal to 0,02 mass%.
- Table 4 and Figure 3 show the relationship between the settling time and solids content of this tar-solvent mixture.
- the solid material removed from the crude tar consists mainly of fine coal particles. On ashing this material at 900 °C, a typical coal ash composition is analysed as shown in Table 5.
- the procedure comprised using a solvent, as per table 2 above, to solvate tar from the solids and to allow the settling of the solids into a water phase.
- RectisolTM Naphta of table 2 was mixed with crude tar feed in a 1 : 1 mass ratio.
- Different wetting-and demulsifying agents were dosed at respective levels of 10-, 30 and 50 ⁇ l per liter of the hydrocarbon phase.
- the solids were then allowed to migrate by settling into the water phase using a retention time of 60 minutes.
- the hydrocarbon phase was analysed for solids content by igniting a known portion of the hydrocarbon phase, thus allowing it to burn in order to remove excess of carbonaceous material.
- the residue obtained in this manner was further ashed at 600 °C for 2 hours.
- the amount of final residue obtained was measured and expressed as mass% solids to be present in the hydrocarbon phase.
- a blank run was included without addition of any wetting or demulsifier agent.
- Table 6 Solids Content Of Hydrocarbon Phase Treated With Different Wetting- And Demulsifying Agents
- Table 7 Solids Content of Tar Fraction Alone After Treatment Calculated From Table 1 Note; Value in Table below is obtained by multiplying average value in Table 6 by 2
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
ZA200102251 | 2001-06-18 | ||
ZA2001/2251 | 2001-06-18 |
Publications (1)
Publication Number | Publication Date |
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WO2002102938A1 true WO2002102938A1 (en) | 2002-12-27 |
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Application Number | Title | Priority Date | Filing Date |
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PCT/ZA2002/000101 WO2002102938A1 (en) | 2001-06-18 | 2002-06-14 | Method of separating particles from a hydrocarbon composition |
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2008080303A1 (en) * | 2006-12-27 | 2008-07-10 | China Petroleum & Chemical Corporation | Hydrogenation and catalytic cracking combined process for residual oil |
US9260667B2 (en) | 2007-12-20 | 2016-02-16 | China Petroleum & Chemical Corporation | Combined process of hydrotreating and catalytic cracking of hydrocarbon oils |
US9834730B2 (en) | 2014-01-23 | 2017-12-05 | Ecolab Usa Inc. | Use of emulsion polymers to flocculate solids in organic liquids |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3684699A (en) * | 1971-02-10 | 1972-08-15 | Univ California | Process for recovering oil from tar-oil froths and other heavy oil-water emulsions |
US4264453A (en) * | 1980-01-10 | 1981-04-28 | Pori International, Inc. | Reclamation of coking wastes |
EP0283584A1 (en) * | 1987-03-23 | 1988-09-28 | Rütgerswerke Aktiengesellschaft | Process for reducing the water and ash content in crude tar |
US4812225A (en) * | 1987-02-10 | 1989-03-14 | Gulf Canada Resources Limited | Method and apparatus for treatment of oil contaminated sludge |
DE4233584A1 (en) * | 1992-03-12 | 1993-09-16 | Preussag Noell Wassertech | Hydrocarbon contg. inorganic sludge sepn. - esp. for treating settling pond sludge in bitumen prodn. from tar sands |
DE4208182A1 (en) * | 1992-03-12 | 1993-09-16 | Preussag Noell Wassertech | Hydrocarbon-contg. mixt. sepn. by solvent extn. - esp. for treating oil sludge from bitumen prodn. from tar sands |
US5989436A (en) * | 1996-01-31 | 1999-11-23 | Mitsubishi Jukogyo Kabushiki Kaisha | Method and device for dehydrating heavy oils |
US6019888A (en) * | 1998-02-02 | 2000-02-01 | Tetra Technologies, Inc. | Method of reducing moisture and solid content of bitumen extracted from tar sand minerals |
-
2002
- 2002-06-14 WO PCT/ZA2002/000101 patent/WO2002102938A1/en not_active Application Discontinuation
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3684699A (en) * | 1971-02-10 | 1972-08-15 | Univ California | Process for recovering oil from tar-oil froths and other heavy oil-water emulsions |
US4264453A (en) * | 1980-01-10 | 1981-04-28 | Pori International, Inc. | Reclamation of coking wastes |
US4812225A (en) * | 1987-02-10 | 1989-03-14 | Gulf Canada Resources Limited | Method and apparatus for treatment of oil contaminated sludge |
EP0283584A1 (en) * | 1987-03-23 | 1988-09-28 | Rütgerswerke Aktiengesellschaft | Process for reducing the water and ash content in crude tar |
DE4233584A1 (en) * | 1992-03-12 | 1993-09-16 | Preussag Noell Wassertech | Hydrocarbon contg. inorganic sludge sepn. - esp. for treating settling pond sludge in bitumen prodn. from tar sands |
DE4208182A1 (en) * | 1992-03-12 | 1993-09-16 | Preussag Noell Wassertech | Hydrocarbon-contg. mixt. sepn. by solvent extn. - esp. for treating oil sludge from bitumen prodn. from tar sands |
US5989436A (en) * | 1996-01-31 | 1999-11-23 | Mitsubishi Jukogyo Kabushiki Kaisha | Method and device for dehydrating heavy oils |
US6019888A (en) * | 1998-02-02 | 2000-02-01 | Tetra Technologies, Inc. | Method of reducing moisture and solid content of bitumen extracted from tar sand minerals |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2008080303A1 (en) * | 2006-12-27 | 2008-07-10 | China Petroleum & Chemical Corporation | Hydrogenation and catalytic cracking combined process for residual oil |
US8529753B2 (en) | 2006-12-27 | 2013-09-10 | Research Institute Of Petroleum Processing, Sinopec | Combined process for hydrotreating and catalytic cracking of residue |
US9260667B2 (en) | 2007-12-20 | 2016-02-16 | China Petroleum & Chemical Corporation | Combined process of hydrotreating and catalytic cracking of hydrocarbon oils |
US9309467B2 (en) | 2007-12-20 | 2016-04-12 | China Petroleum And Chemical Corp. | Integrated process for hydrogenation and catalytic cracking of hydrocarbon oil |
US9834730B2 (en) | 2014-01-23 | 2017-12-05 | Ecolab Usa Inc. | Use of emulsion polymers to flocculate solids in organic liquids |
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