WO2013153452A2 - Process of reducing viscosity of heavy crude oil by removal of asphaltene using a precipitating agent - Google Patents
Process of reducing viscosity of heavy crude oil by removal of asphaltene using a precipitating agent Download PDFInfo
- Publication number
- WO2013153452A2 WO2013153452A2 PCT/IB2013/001061 IB2013001061W WO2013153452A2 WO 2013153452 A2 WO2013153452 A2 WO 2013153452A2 IB 2013001061 W IB2013001061 W IB 2013001061W WO 2013153452 A2 WO2013153452 A2 WO 2013153452A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- precipitant
- oil
- crude oil
- stream
- upgraded
- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/302—Viscosity
Definitions
- the invention is generally directed to reducing the viscosity of heavy and extra heavy crude oils, and more particularly to a process for reducing the viscosity of heavy and extra heavy crude oils by means of total or partial oil deasphalting using a precipitating agent in order to obtain an upgraded crude oil of lower viscosity that can be pumped without the use of diluents.
- the upgrading also includes a reduction in metals and sulfur associated with asphaltene removal.
- the process consists of relatively simple equipment such as static mixers and stirred tanks and operation temperature is low and pressure is moderate.
- Crude oil contains four different hydrocarbons including paraffins, napthenes, aromatics, and asphaltenes.
- Paraffins, or alkanes are saturated hydrocarbons that consist only of hydrogen and carbon atoms, having the general formula C n H2 n +2. All bonds are single bonds, and the carbon atoms are not joined in cyclic structures but instead form a simple chain. They make up from about 15 to about 60% of crude oil, and on average about 30%.
- Resins or naphthenes, otherwise known as cycloalkanes are alkanes that have one or more rings of carbon atoms in the chemical structure of their molecules. They make up from about 30 to about 60% of crude oil, and on average about 49%.
- Aromatics, or arenes are hydrocarbons with alternating double and single bonds between carbon atoms forming rings. Aromatics make up from about 3 to about 30%) of crude oil, and on average about 15%>.
- Asphaltenes consist primarily of carbon, hydrogen, nitrogen, oxygen, and sulfur, as well as trace amounts of vanadium and nickel.
- the C:H ratio is approximately 1 : 1.2, depending on the asphaltene source.
- Asphaltenes are defined operationally as the n-heptane (C 7 Hi 6 )-insoluble, toluene (C 6 H 5 CH 3 )-soluble component of a carbonaceous material such as crude oil, and are the sticky, black, highly viscous residue of distillation processes. They make up the remainder of crude oil, and on average from about 3 to about 10% of the crude oil; however heavy oils can contain 10% or more, with a high C:H ratio. Due to the aggregation of asphaltenes, they are the most significant contributor to the viscosity of crude oil affecting its viscosity.
- Light crude oil is liquid petroleum that has low viscosity, low specific gravity, and high API (American Petroleum Institute) gravity due to the presence of a high proportion of light hydrocarbon fractions. API gravity is calculated by dividing 141.5 by the fluid's specific gravity and subtracting 131.5.
- the New York Mercantile Exchange (NYMEX) defines light crude oil for domestic U.S. oil as having an API gravity between 37° API (840 kg/m 3 ) and 42° API (816 kg/m 3 ), while it defines light crude oil for non- U.S. oil as being between 32° API (865 kg/m 3 J ) and 42° API (816 kg/m ).
- the National Energy Board of Canada defines light crude oil as having a density less than 875.7 kg/m (more than 30.1° API).
- Pemex defines light crude oil as being between 27° API (893 kg/m 3 ) and 38° API (835 kg/m 3 ).
- heavy crude oils are generally not pumpable due to the high viscosity. Therefore, it is advantageous to remove the higher viscosity products, i.e. asphaltenes, in order to pump the remaining, lighter deasphalted crude oil.
- Light crude oil is also desired over heavy crude oil because it receives a higher price than heavy crude oil on commodity markets because it produces a higher percentage of gasoline and diesel fuel when converted into products by an oil refinery.
- Deasphalting is a well-known process that uses extraction towers and usually propane as a solvent as depicted in a number of references including, for example, U.S. Patent Nos.
- the list is not exhaustive but shows that many types of solvents have been used.
- One specific process to produce fluid catalytic cracking (FCC) feedstock can use lower range solvent to crude oil ratios between 1 : 1 to 4: 1 by volume, as described in U.S. Patent No. 5,000,838, but in this process, the solvent recovery is not complete.
- FCC fluid catalytic cracking
- the solvent type is related to the yield and quality of the upgraded oil (hereinafter "UO"). In general, a process with propane gives lower yields of UO, but of better quality regarding lighter density and lower metals content.
- the solvent is subjected to special operating conditions, which changes the solubility and its precipitating power.
- special operating conditions which changes the solubility and its precipitating power.
- diluents are diluting agents that thin, or reduce the viscosity of a fluid to which it is added. For example, diluents are added to and blended with the heavy crude oil at the oilfield. The lower viscosity solution is then pumped, trucked, and/or transported to a refinery, storage facility, or other desired location, where the solution is broken to separate the crude oil from the diluent. The diluent is then pipelined or otherwise transported back for reuse. However, this process requires additional process steps, such as returning the diluent, that can be costly. Also, available diluents, such as naphtha, are becoming increasingly unavailable.
- Embodiments of the present invention described many of the drawbacks inherent in the processes described above. Embodiments are directed to a process that reduces heavy and extra heavy crude oil viscosity by partial or total deasphalting of such crude oils producing a high yield of the partially or totally deasphalted product at the oilfield.
- the process can significantly reduce, or in a best case scenario, completely eliminate the use of diluents for pipeline transport of crude oil.
- the process is designed so that it can be readily implemented in oilfield operations sites requiring moderate pressures and temperatures.
- the present invention includes a process that uses a low precipitant/crude oil ratio, such as, for example, a 2: 1 in volume ratio or less, and a 1.5: 1 in weight ratio or less, and more particularly about 1 : 1, compared to ratios of 8: 1 in weight or more of the prior art, to produce upgraded oil with a viscosity suitable for pumping at ambient temperatures, while maximizing upgraded oil yield, such as, for example, about 90% or greater volumetric recuperation, and more particularly about 94% or greater.
- the process also produces a reduction in metal and sulfur content of the upgraded oil obtained related to the asphaltene removal.
- the upgraded oil also has an API gravity at least about three degrees or more greater than an API gravity of the heavy crude oil.
- precipitant and crude oil come into intimate contact with a static mixer arrangement, at temperatures below 80 °C (176 °F) and pressures between 40 and 60 psig.
- the crude oil/precipitant stream is then taken to an agitated tank for further mixing and for ensuring sufficient residence time in order to improve solid precipitation.
- the agitated tank content is then drained out of the tank using suitable equipment that forces it to flow into a high gravity field device (a hydro-cyclone or a centrifuge).
- a high gravity field device a hydro-cyclone or a centrifuge
- the crude oil/precipitant stream is separated into two currents: a solid free stream and high solid content slurry which still contains some upgraded oil and precipitant.
- the solid free stream is fed to a flash separator that recovers the precipitant to be reused, and produces the upgraded oil.
- the high solid content stream goes to a "washing" section were the solids are washed to recuperate the liquid that remains occluded in them. This step is critical to increase the volumetric yield of the process.
- the washed product goes to a high gravitational force separator (centrifuge) where two streams are obtained: one rich in solids (asphaltenes) that goes to a dryer where the remaining precipitant is recuperated, and a second current comprising, or alternatively consisting of, dry solids that can be used for power generation (combustion) or other purposes.
- the second stream is a liquid that contains some crude oil and precipitant that goes to the flash unit to recover the lighter precipitant and to produce the upgraded oil, which is mixed with the oil obtained in the first separator.
- the precipitant remaining in the upgraded oil is adjusted to further reduce viscosity, if required.
- the precipitant used in this process is a light fraction of crude oil, like light gasoline, that reduces asphaltene solubility in the crude oil and that can optionally contain some additives (paraffinic, aromatic or oxygenated compounds) that enhance the performance of the process as required.
- the formulation of the precipitant is such that it fits the type of crude being treated, as well as the required quality and yield.
- An alternative embodiment of the process includes a battery of static mixers that blends the extra heavy and heavy crude oil feed with the stream that leaves the washing section.
- the precipitant enters the washing section, which consists of a stirred tank and a centrifuge or hydro-cyclones; the solid stream of the centrifuge goes to a dryer where solids are obtained as a product and precipitant is recovered.
- the liquid stream of the centrifuge goes to the static mixers where it combines with crude oil as mentioned.
- the crude oil and precipitant blend that exits the static mixers goes to an agitated tank to provide for residence time and then to a separator (hydro -cyclones or centrifuge) where the liquid stream goes to a flash separator where the precipitant is recuperated while the bottom stream goes to a steam stripper to recover the last traces of solvent (if required). From the bottom of the stripper, upgraded crude oil is obtained.
- the heavy stream of the separator goes to the washing section or stirred tank where precipitant and make-up precipitant are introduced. From there the combined stream goes to the washing section centrifuge.
- Figure 1 is a diagram showing in a schematic way the main stages of the process of upgrading the crude oil for transport in pipelines, according to an embodiment of the invention.
- Figure 2 shows a diagram of a modified version of the process for upgrading crude oil for pipeline transport.
- a process 1000 is shown in which crude oil (1) is blended with a feed precipitant (2) in a set of static mixers (3).
- the feed crude oil (1) generally comprises a kinematic viscosity (dynamic viscosity divided by fluid density) of about 2400 centistokes (cSt) or more.
- cSt centistokes
- water has been removed from the crude oil before being introduced into process 1000.
- the crude oil (1) is at a temperature range of 50 to 100 °C (122 to 212 °F), with pressures lower than 60 psig and the volumetric precipitant to oil volume ratio is in a range from about 1 to 1 to about 1 to 2, including for example, 1.25: 1 and 1.5: 1, depending on density differences.
- the weight ratio of crude oil to precipitant (or solvent) can comprise about 1 : 1.
- the crude oil/precipitant mix is introduced to a stirred tank (4) to allow for some residence time and growth of the precipitated particles.
- the use of light precipitant with relatively low boiling points (FBP less than 140 °C or 284 °F) helps in the separation and precipitation of asphaltenes.
- the asphaltenes are generally present in the agitated tank (4) as suspended particles and nano-colloids.
- the separator (6) uses inertial forces to separate the solid particles from the liquid upgraded crude oil.
- the separator (6) can comprise, for example, one or more hydro- cyclones or centrifuges. Precipitant is present in both streams.
- the liquid exits through line 7 to a "flash" separator or distillation tower (8) to recuperate the precipitant from the upgraded oil.
- the "flash" separator (8) operates at a pressure slightly higher than atmospheric and temperatures capable of recuperating most of the precipitant. If needed, the flash tower or separator (8) operation can be adjusted so that a convenient amount of precipitant remains in the upgraded oil, to further reduce viscosity as required or desired.
- the precipitant leaves the flash through line 9 to be cooled down in condensers (not shown) exiting at 35 - 55 °C (95 - 131 °F) and then goes through line 17 to a solvent tank (18). From tank (18), the precipitant goes through line 19 to line 2 and is recycled and mixed with crude oil (1).
- the bottom of the flash drum goes through line 20 into an optional steam stripper (21) that operates to recuperate traces of precipitant left in the upgraded oil, if required or desired.
- the recuperated precipitant plus steam mix leave the stripper (21) through line 24, where the mix is condensed (not shown) and the water and precipitant are separated in a drum (not shown).
- the recuperated precipitant goes through line 17 where it mixes with the precipitant from line 9 of the flash separator 8, and the combined currents return to the solvent tank (18) as described above. From the precipitant tank (18), the solvent transits line 19 into line 2 and it is finally mixed with crude oil (1).
- vapor in the form of steam, enters the stripper (21) through line 23.
- the product of the stripper (21) is the lower viscosity upgraded oil, which exits through line 22.
- the kinematic viscosity (dynamic viscosity divided by the density of the fluid) is equal to or less than about 700 centistokes (cSt).
- the yield of crude oil in the upgraded oil is about 92% or greater in volume. It has been observed that the initial viscosity of the crude oil feed (1) is independent from, and does not affect, the yield of upgraded oil.
- the liquid/solid stream, or oil slurry containing the asphaltenes that leaves the first separator (6) through line 10 goes to an agitated tank (11) where it is very well mixed or washed with precipitant at low shear rates fed from recycle stream 19 through line 25 with a volumetric flow similar to the one used in the first contact in the static mixers (3).
- the mixture of the oil slurry and the precipitant leaves the agitated tank (11) through line 12 to a centrifugal separator (13) that operates between 1000 to 6000 g's.
- the combination of the tank (11) and separator (13) make up the washing unit of the process, and is shown in Figure 1 inside a dashed box.
- a dry stream (26), containing mostly asphaltenes (26), can be used to produce energy, such as by firing at the oilfield site, or for other purposes.
- precipitant make-up or additives are introduced, as needed, such as at start-up, through line 27 that combines with recycled precipitant 19 at line 2, where it ultimately mixes with the crude oil in line 1.
- a process 2000 includes a crude oil feed (50) mixed with a recycled current (51) that contains precipitant and deasphalted crude oil recuperated in the washing section exiting the separator (52).
- This mixture goes through a static mixers battery (53) and then enters a stirred tank (54) to allow for residence time. From there, the liquid-solid mixture exits through line (55) to end in a separation unit (56), which can comprise a battery of hydro-cyclones or centrifuges.
- Two streams leave the separator (56); one liquid stream (57) goes to a flash separator unit or distillation tower (58) where the solvent (i.e. light precipitant) leaves through line 59 to precipitant tank (60).
- the heavy fraction or oil slurry leaves the separator (56) through line 61 to the wash tank (62) of a wash unit shown in dotted lines, where it is washed with precipitant from precipitant tank 60 via line 71. From the wash tank (62) the stream exits through line (63) to the separator (52) of the wash unit. The separator (52) discharges the liquid recycled current (51) that goes to blending with the crude oil as aforementioned.
- the slurry or heavy fraction leaves the separator (52) through line 64 to the dryer (65).
- the dryer output consists of two currents: stream 66, which is the solid product comprising mainly asphaltenes, similar to line 26 of Figure 1; and stream (67), which is recuperated precipitant.
- This recuperated precipitant is condensed (condensing section not shown) and sent to a precipitant tank (60) where it is blended with recuperated precipitant (59) from flash unit or distillation tower (58) and fed via line 71 to wash tank (62) as described above.
- the bottom of the flash tower (58) leaves through line 68 to an optional stripper (69) where the current 68 containing crude oil and precipitant is stripped with steam (70). From the bottom of the stripper the upgraded oil (72) is obtained.
- the recuperated precipitant plus steam leave the stripper through line 74 where it is condensed and the water and solvent separated in a drum (not shown).
- the precipitant is sent through line 59 to precipitant tank (60).
- precipitant make-up or additives are introduced, as needed, such as into wash agitated tank 62, through line 76.
- the kinematic viscosity (dynamic viscosity divided by the density of the fluid) of the upgraded oil at 72 is equal to or less than about 700 centistokes (cSt).
- the yield of crude oil in the upgraded oil is about 92 % or greater in volume. It has been observed that the initial viscosity of the crude oil feed (50) is independent from, and does not affect, the yield of upgrade oil.
- the ratios of precipitant to crude oil at the feed of process 2000 is also similar to process 1000 of Figure 1, and can comprise, for example, a volumetric precipitant to oil volume ratio is in a range from about 1 to 1 to about 1 to 2, including for example, 1.25: 1 and 1.5: 1, depending on density differences.
- the weight ratio of crude oil to precipitant (or solvent) can comprise about 1 : 1.
- the precipitant can comprise, for example, a light or natural gasoline.
- the precipitant's precipitating properties can be modified using optional additives such as light paraffmic hydrocarbons (pentane, hexane and heptanes, for example) or oxygenated hydrocarbons (such as pentanol, butanol, light ketones) that can be added through line 27 in Figure 1, or line 76 in figure 2).
- the formulation of the final precipitant is a function of the type of crude oil and the level of deasphalting required in the process to reach a low enough upgraded oil viscosity for pipe transportation and the highest yield possible.
- the vapor pressure of the solvent or precipitant must be such as to allow an easy separation in the flash columns or distillation column of the processes.
- the stripper is used to recuperate traces of solvent from the upgraded product; however, depending on the user's needs, the stripper could be omitted from the process.
- the washed product is separated in a centrifuge at 4000 g's and two streams are obtained: a slurry stream of 40.8 g rich in asphaltenes (18.0 %), very little crude oil (6.5 %) and precipitant (75.5 %) and a liquid stream of 118.1 g that contains washed crude oil (20.3 %) and solvent (79.7%).
- the slurry stream is dried and 10 g of solids are obtained and 30.8 g of precipitant are recuperated.
- the liquid stream goes to the flash tower, were it is mixed with the liquid stream from the fist centrifuge. From the flash unit, 169.1 g of the precipitant is recuperated and 90.0 g of upgraded oil are obtained as a product (characteristics shown in table 1).
- the process has a very high yield of product (90.0 % wt) and a volumetric recuperation of 92 %. There is also a substantial reduction in metals.
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- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
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Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
MX2014012216A MX2014012216A (en) | 2012-04-10 | 2013-04-09 | Process of reducing viscosity of heavy crude oil by removal of asphaltene using a precipitating agent. |
CA2867793A CA2867793A1 (en) | 2012-04-10 | 2013-04-09 | Process of reducing viscosity of heavy crude oil by removal of asphaltene using a precipitating agent |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US201261622197P | 2012-04-10 | 2012-04-10 | |
US61/622,197 | 2012-04-10 | ||
US13/835,104 | 2013-03-15 | ||
US13/835,104 US20130264247A1 (en) | 2012-04-10 | 2013-03-15 | Process of reducing viscosity of heavy crude oil by removal of asphaltene using a precipitating agent |
Publications (2)
Publication Number | Publication Date |
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WO2013153452A2 true WO2013153452A2 (en) | 2013-10-17 |
WO2013153452A3 WO2013153452A3 (en) | 2014-01-16 |
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Family Applications (1)
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PCT/IB2013/001061 WO2013153452A2 (en) | 2012-04-10 | 2013-04-09 | Process of reducing viscosity of heavy crude oil by removal of asphaltene using a precipitating agent |
Country Status (6)
Country | Link |
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US (1) | US20130264247A1 (en) |
CA (1) | CA2867793A1 (en) |
CO (1) | CO7121326A2 (en) |
MX (1) | MX2014012216A (en) |
PE (1) | PE20142303A1 (en) |
WO (1) | WO2013153452A2 (en) |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10640716B2 (en) | 2014-05-30 | 2020-05-05 | Fluor Technologies Corporation | Configurations and methods of dewatering crude oil |
CA2963436C (en) | 2017-04-06 | 2022-09-20 | Iftikhar Huq | Partial upgrading of bitumen |
US10954454B2 (en) | 2017-08-21 | 2021-03-23 | Saudi Arabian Oil Company | Non-solvent crude oil heavy oil stream de-asphalting process |
US10308880B2 (en) | 2017-08-21 | 2019-06-04 | Saudi Arabian Oil Company | Non-solvent asphaltene removal from crude oil using solid heteropoly compounds |
US11248174B2 (en) | 2019-12-27 | 2022-02-15 | Saudi Arabian Oil Company | Process to remove asphaltene from heavy oil by solvent |
US11225617B1 (en) | 2020-06-25 | 2022-01-18 | Saudi Arabian Oil Company | Continuous catalytic deasphalting process |
WO2022187124A1 (en) | 2021-03-01 | 2022-09-09 | Saudi Arabian Oil Company | Integrated process with a deasphalting column for crude oil direct catalytic upgrading |
EP4288513A1 (en) | 2021-03-01 | 2023-12-13 | Saudi Arabian Oil Company | Integrated process with a depolyaromatization column for the production of benzene, toluene and xylenes from pyrolysis fuel oil stream |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3159571A (en) * | 1960-11-28 | 1964-12-01 | Shell Oil Co | Residual oil refining process |
EP0134088A1 (en) * | 1983-07-06 | 1985-03-13 | The British Petroleum Company p.l.c. | Treatment of viscous crude oil |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
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US20090139906A1 (en) * | 2007-11-30 | 2009-06-04 | Jan Kruyer | Isoelectric separation of oil sands |
WO2013019418A2 (en) * | 2011-07-29 | 2013-02-07 | Saudi Arabian Oil Company | Process for stabilization of heavy hydrocarbons |
-
2013
- 2013-03-15 US US13/835,104 patent/US20130264247A1/en not_active Abandoned
- 2013-04-09 MX MX2014012216A patent/MX2014012216A/en unknown
- 2013-04-09 CA CA2867793A patent/CA2867793A1/en not_active Abandoned
- 2013-04-09 PE PE2014001466A patent/PE20142303A1/en not_active Application Discontinuation
- 2013-04-09 WO PCT/IB2013/001061 patent/WO2013153452A2/en active Application Filing
-
2014
- 2014-10-30 CO CO14240738A patent/CO7121326A2/en unknown
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3159571A (en) * | 1960-11-28 | 1964-12-01 | Shell Oil Co | Residual oil refining process |
EP0134088A1 (en) * | 1983-07-06 | 1985-03-13 | The British Petroleum Company p.l.c. | Treatment of viscous crude oil |
Also Published As
Publication number | Publication date |
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CA2867793A1 (en) | 2013-10-17 |
CO7121326A2 (en) | 2014-11-20 |
WO2013153452A3 (en) | 2014-01-16 |
MX2014012216A (en) | 2014-11-25 |
US20130264247A1 (en) | 2013-10-10 |
PE20142303A1 (en) | 2015-01-16 |
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