CA3038209A1 - System and method for solvent de-asphalting - Google Patents

Abstract

A de-asphalting system for solvent de-asphalting including a desasphalter and a controller. The deasphalter defines a contacting zone and a separation zone. The contact zone contacts a feed, including asphaltenes, and a solvent to form a mixture, where the contacting of the feed and the solvent causes at least a portion of the asphaltenes to precipitate out of the mixture. The contacting is disposed at an operating temperature. The separation zone separates the mixture into a de-asphalted oil-comprising material fraction ("S+PDAO") and a asphaltene-rich material fraction. The asphaltene-rich material fraction includes the precipitated asphaltenes. The controller controls at least one operating parameter of the deasphalter based on at least on a refractive index of the S+PDAO phase. The operating parameter is selected from: the operating temperature; the composition of the feed; the composition of the solvent; a ratio of the mass of precipitated asphaltenes to the mass of asphaltenes within the feed; and a ratio of the mass of the solvent to the mass of the feed.

Description

SYSTEM AND METHOD FOR SOLVENT DE-ASPHALTING
FIELD
[0001] The invention relates to a process for upgrading heavy oil and/or bitumen.
Specifically, the process relates to a process for de-asphalting heavy oil and/or bitumen.
BACKGROUND

[0002] Heavy oil and/or bitumen are often difficult to transport from production sites due to high viscosities at typical handling temperatures. They generally need to be diluted by the addition of at least one low density and low viscosity diluent to make the heavy oil and/or bitumen transportable, particularly when transporting over long distances.

[0003] There are several disadvantages of adding diluent to heavy oil and/or bitumen to produce transportable oil including: availability of diluents, typically light hydrocarbons, such as gas condensates, is steadily decreasing worldwide, making them more expensive to procure;
and the diluent takes up pipeline space without adding value.

[0004] For example, in Canada, when making transportable oil and using gas condensate as a diluent, the volume of gas condensate added to the bitumen is typically 30 to 35% of the total product.

[0005] One method for addressing the difficulties for handling heavy oil and/or bitumen is solvent de-asphalting. Solvent de-asphalting is a process that removes the asphaltenes fraction from a hydrocarbon feed using a solvent. Solvent de-asphalting is described in, and amongst other sources, the article by Billon and others published in 1994 in Volume 49, No. 5 of the journal of the French Petroleum Institute, pages 495 to 507, in the book "Raffinage et conversion des produits lourds du petrole [Refining and Conversion of Heavy Petroleum Products]" by J. F. Le Page, S. G. Chatila, and M. Davidson, Edition Technip, pages 17-32.
Exemplary solvent extraction processes, for effecting the de-asphalting, are described in U.S.
Patent No. 7,597,794.

[0006] When the solvent is mixed with the hydrocarbon feed in an extractor, asphaltenes (which are insoluble in certain solvents) precipitate from the mixture. These precipitated asphaltenes are recovered from the bottom of the extractor, while the remaining hydrocarbons are recovered along with the solvent from the top of the extractor. The solvent is then separated from the remaining hydrocarbons. This asphaltene-lean hydrocarbon stream has improved properties compared to the original hydrocarbon feed due to the reduction or elimination of undesirable asphaltenes.

[0007] JS Buckley et al, "Asphaltene Precipitation and Solvent Properties of Crude Oils", (1998) 16:3-4 Petrol Sci and Tech 251 show that the prediction of the onset of asphaltene precipitation at ambient conditions may be improved using refractive index (RI) to characterize crude oils and their mixtures with precipitants and solvents. However, Buckley does not teach the significance of RI at solvent de-asphalting process conditions, which occur after the onset of precipitation and at higher temperatures and pressures.

[0008] K Akbarzadeh et al, "A generalized regular solution model for asphaltene precipitation from n-alkane diluted heavy oils and bitumens", (2005) 232 Fluid Phase Equilibria 159 discloses a solvent de-asphalting model. However, these models are not very robust, rely on parameters that cannot be easily measured or estimated, and have low accuracy.

[0009] There exists a need for improved solvent de-asphalting systems and methods.
SUMMARY

[0010] In one aspect, there is provided a method for solvent de-asphalting including selecting a solvent based on RI and contacting the selected solvent with a feed including asphaltenes to effect de-asphalting.

[0011] In another aspect, there is provided a de-asphalting system for solvent de-asphalting including a deasphalter and a controller. The deasphalter defines a contacting zone for contacting a feed, including asphaltenes, and a solvent to form a mixture, where the contacting of the feed and the solvent causes at least a portion of the asphaltenes to precipitate out of the mixture, the contacting disposed at an operating temperature; and a separation zone to separate the mixture into a de-asphalted oil-comprising material fraction ("S+PDA0") and a asphaltene-rich material fraction, the asphaltene-rich material fraction including the precipitated asphaltenes. The controller controls at least one operating parameter of the deasphalter based on at least on a refractive index of the S+PDA0 phase. The operating parameter is selected from: the operating temperature; the composition of the feed; the composition of the solvent; a ratio of the mass of precipitated asphaltenes to the mass of asphaltenes within the feed; and a ratio of the mass of the solvent to the mass of the feed.

[0012] In some embodiments, the de-asphalting system further includes at least one flow regulator operatively connected to the controller for controlling a feed flow rate of the feed, a solvent flow rate of the solvent or both.

[0013] In some embodiments, the de-asphalting system further includes a temperature regulator operatively connected to the controller for controlling the operating temperature of the contacting zone.

[0014] In some embodiments, the de-asphalting system further includes a refractive index determining device operatively connected to the controller for determining the refractive index of the S+PDAO.

[0015] In some embodiments, the refractive index determining device is a refractometer.
In some embodiments, the refractive index determining device is a densitometer.

[0016] In some embodiments, the refractive index of the S+PDAO is calculated as a function of the portion of the precipitated asphaltenes, the refractive index of the feed composition, the refractive index of the solvent, the UOP-K characterization factor of the solvent, and the operating temperature according to the following formulas:
mpach R'S+PDAO @TT RIS+PDA00 @rc -F slope x niC5¨asphaltenes ;
'"Feed RI S+PDA00 @TT = Ao + (A1 x RIFeed@Toc +A2 X RI
--Solvent @TT) X "P-KSAolvõt; and slope = A4 + (A5 X RIFeed @Toc + A6 X RISolvent @T C) X U 13-1CsA071vent=

[0017] In another aspect, there is provided a method for solvent de-asphalting including providing a feed, including asphaltenes, at a feed flow rate; providing a solvent at a solvent flow rate; contacting the solvent and the feed at an operating temperature to effect precipitation of at least a portion of the asphaltenes to obtain a S+PDAO and an asphaltene-rich material fraction, where the asphaltene-rich material fraction, includes the precipitated asphaltenes; and controlling one operating parameter based on at least a refractive index of the S+PDAO, the operating parameter selected from: the operating temperature, the composition of the feed, the composition of the solvent, a ratio of the precipitated asphaltenes to the mass of asphaltenes within the feed, and a ratio of the feed flow rate to the solvent flow rate.

[0018] In another aspect, there is provided a deasphalted oil obtained by a method including the steps of: providing a feed, including asphaltenes, at a feed flow rate; providing a solvent at a solvent flow rate; contacting the solvent and the feed at an operating temperature to effect precipitation of at least a portion of the asphaltenes to obtain a S+PDA0 and an asphaltene-rich material fraction, wherein the asphaltene-rich material fraction includes the precipitated asphaltenes; and controlling one operating parameter based on at least a refractive index of the S+PDAO, the operating parameter selected from: the operating temperature, the composition of the feed, the composition of the solvent, a ratio of the precipitated asphaltenes to the mass of asphaltenes within the feed, and a ratio of the feed flow rate to the solvent flow rate.

[0019] In another aspect, there is provided a method for solvent de-asphalting including:
defining at least the following operating parameters: a composition of a feed including asphaltenes, a target ratio of a mass of removed asphaltenes to the mass of asphaltenes within the feed, an operating temperature for contacting the feed and a solvent, and a ratio of a feed flow rate of the feed to a solvent flow rate of the solvent; determining an RI
of the solvent based at least on calculating the RI of a S+PDA0 formed by contacting the feed with the solvent;
selecting a solvent based at least on the determined solvent RI; and contacting the selected solvent with the feed at the operating parameters to effect de-asphalting.

[0020] In another aspect, there is provided a method for starting up a solvent deasphalting process including: pre-determining four operating parameters, the operating parameters are selected from: an operating temperature, a composition of a feed, a composition of a solvent, a target ratio of a mass of precipitated asphaltenes to a mass of asphaltenes initially within the feed, and a ratio of a feed flow rate to a solvent flow rate; determining the non-predetermined operating parameter based on at least an expected RI of an S+PDA0 stream generated by the process; and starting up the process using the pre-determined operating parameters and the determined operating parameter.
BRIEF DESCRIPTION OF DRAWINGS

[0021] Figure 1 shows a system for de-asphalting according to an embodiment.

[0022] Figure 2 shows a method for de-asphalting according to an embodiment.

[0023] Figure 3 shows a product obtained by a method for de-asphalting according to an embodiment.

[0024] Figure 4 shows a method for de-asphalting according to an embodiment.
DETAILED DESCRIPTION

[0025] This disclosure is based in part on the surprising discovery that a solvent de-asphalting process can be characterized and/or controlled based at least on refractive index ("RI") of a product stream.

[0026] In one aspect, there is provided a system for de-asphalting 100 (Figure 1). The de-asphalting system 100 includes a deasphalter 101. A feed 104, including asphaltenes 104a, and a solvent 106 are contacted within a contacting zone 103 of the deasphalter 101 to form an intermediate mixture 107. The contacting zone 103 is disposed at an operating temperature.
The asphaltenes 104a are insoluble in the solvent 106, and at least a portion of the asphaltenes 110a will precipitate out of the mixture 107. The mixture 107, resulting from the contacting, is separated in a separation zone 109 of the deasphalter 101, into at least a deasphalted oil-comprising material fraction ("S+PDA0") 108 and an asphaltene-rich material fraction 110. In this context, the use "at least" suggests that there may be other fractions that are also separated. The asphaltene content of the deasphalted oil-comprising material fraction 108 is less than the asphaltene content of the feed 104. The asphaltene-rich material fraction 110 includes the precipitated asphaltenes 110a.

[0027] The de-asphalting system 100 includes a controller 112 for controlling at least one operating parameter of the de-asphalting system 100 based on at least a RI
of the S+PDA0 108. The operating parameter is selected from: the operating temperature; the composition of the feed 104; the composition of the solvent 106; a ratio of the mass of the precipitated asphaltenes 110a to the mass of the asphaltenes 104a within the feed; and a ratio of the mass of the solvent 106 to the mass of the feed 104.

[0028] In some embodiments, the feed 104 is a heavy hydrocarbon-comprising material.
The heavy-hydrocarbon-comprising material may be liquid, semi-solid, or solid, or any combination thereof.

[0029] In some embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 10 weight percent of hydrocarbon-comprising material that boils above 500 C. In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 20 weight percent of hydrocarbon-comprising material that boils above 500 C. In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 30 weight percent of hydrocarbon-comprising material that boils above 500 C. In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 40 weight percent of hydrocarbon-comprising material that boils above 500 C. In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 50 weight percent of hydrocarbon-comprising material that boils above 500 C.
In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 60 weight percent of hydrocarbon-comprising material that boils above 500 C. In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 70 weight percent of hydrocarbon-comprising material that boils above 500 C. In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 80 weight percent of hydrocarbon-comprising material that boils above 500 C. In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that includes at least 90 weight percent of hydrocarbon-comprising material that boils above 500 C. In some of these embodiments, for example, the heavy hydrocarbon-comprising material is a material that boils above 500 C.

[0030] In some embodiments, for example, the heavy hydrocarbon-comprising material includes a Conradson carbon residue content of at least 12 weight percent, based on the total weight of the heavy hydrocarbon-comprising material. In some of these embodiments, for example, the heavy hydrocarbon-comprising material includes a Conradson carbon residue content of at least 13 weight percent, based on the total weight of the heavy hydrocarbon-comprising material. In some of these embodiments, for example, the heavy hydrocarbon-comprising material includes a Conradson carbon residue content of at least 14 weight percent, based on the total weight of the heavy hydrocarbon-comprising material. In some of these embodiments, for example, the heavy hydrocarbon-comprising material includes a Conradson carbon residue content of less than 30 weight percent, based on the total weight of the heavy hydrocarbon-comprising material.

[0031] In some embodiments, for example, the heavy hydrocarbon-comprising material includes an asphaltene content of less than 40 weight A), based on the total weight of the heavy hydrocarbon-comprising mixture. In some of these embodiments, for example, the heavy hydrocarbon-comprising material includes an asphaltene content of less than 20 weight %, based on the total weight of the heavy hydrocarbon-comprising mixture. In some of these embodiments, for example, the heavy hydrocarbon-comprising material includes an asphaltene content of less than 15 weight %, based on the total weight of the heavy hydrocarbon-comprising mixture.

[0032] In some embodiments, for example, the asphaltenes are C5-asphaltenes.
C5-asphaltenes are material precipitating from a hydrocarbon composition after being mixed with 40 volumes of an n-pentane (n-05) solvent at room temperature. The C5-asphaltene content of the heavy hydrocarbon-comprising material composition can be determined using ASTM D6560, modified to use pentane as the solvent.

[0033] In some embodiments, for example, the heavy hydrocarbon-comprising material includes an inorganic solids content of less than 1 weight %, based on the total weight of the heavy hydrocarbon-comprising mixture. In some of these embodiments, for example, the heavy hydrocarbon-comprising material includes an inorganic solids content of less than 0.5 weight %, based on the total weight of the heavy hydrocarbon-comprising mixture.

[0034] In some embodiments, for example, the inorganic solids of the heavy hydrocarbon-comprising material were micrometer (10-6 m) size particles. In some embodiments, for example, the inorganic solids in the heavy hydrocarbon-comprising material were nanometer (10-9 m) size particles.

[0035] In some embodiments, for example, the heavy hydrocarbon-comprising material has an API (American Petroleum Institute) gravity of less than 20 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API gravity of less than 15 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API
gravity of less than 12 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API gravity of less than 10 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API gravity of less than 5 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API gravity of less than 0 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API

gravity of less than -2 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API gravity of less than -4 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API gravity of less than -8 . In some embodiments, for example, the heavy hydrocarbon-comprising material has an API gravity of less than -10 .

[0036] In some embodiments, for example, the heavy hydrocarbon-comprising material includes, or in some embodiments, consists of, residuum or resid. Exemplary residuum includes various heavy crude and refinery fractions. In this respect, in some embodiments, for example, the heavy hydrocarbon-comprising material includes, or in some embodiments, consists of, fresh resid hydrocarbon feeds, a bottoms stream from any refinery process, such as petroleum atmospheric tower bottoms, vacuum tower bottoms, or a bottoms stream from a coker or a visbreaker or a thermal cracking unit, or a bottoms stream from a FCC or a RFCC unit, hydrocracked atmospheric tower, vacuum tower, FCC, or RFCC bottoms, straight run vacuum gas oil, hydrocracked vacuum gas oil, fluid catalytically cracked (FCC) slurry oils or cycle oils, as well as other similar hydrocarbon-comprising materials, or any combination thereof, each of which may be straight run, process derived, hydrocracked, or otherwise partially treated (for example, desulfurized). The above-described heavy hydrocarbon-comprising material may also include various impurities, such as sulphur, nitrogen, oxygen, halides, and metals.

[0037] In some embodiments, for example, the heavy hydrocarbon-comprising material includes, or in some embodiments, consists of, a crude, such as an heavy and/or an ultra-heavy crude. Crude refers to hydrocarbon material which have been produced and/or retorted from hydrocarbon-containing formations and which has not yet been distilled and/or fractionally distilled in a treatment facility to produce multiple components with specific boiling range distributions, such as atmospheric distillation methods and/or vacuum distillation methods.
Exemplary crudes include coals, bitumen, tar sands, or crude oil. In such embodiments, the crude can be characterized as having a number of separable fractions (or "cuts") that could be separable by distillation, each cut having characterizable properties. In some embodiments, the crude has five cuts: a kerosene fraction, a diesel fraction, a light vacuum gas oil fraction, a heavy vacuum gas oil fraction, and a vacuum residue fraction. In some embodiments, the vacuum residue fraction comprises the asphaltenes.

[0038] In some embodiments, the solvent 106 is a suitable hydrocarbon material which is a liquid at the operating conditions of the solvent material contacting zone. In some embodiments, for example, the solvent is a relatively light hydrocarbon or a mixture including two or more light hydrocarbons. Exemplary light hydrocarbons include propane, butane, isobutane, pentane, isopentane, hexane, heptane, octane, nonane, and corresponding mono-olefinic hydrocarbons, and corresponding cyclic hydrocarbons. In some embodiments, for example, the solvent includes one or more paraffinic hydrocarbons having from 3 to 10 carbon atoms in total per molecule. In some embodiments, for example, the solvent is pentane. In some embodiments, the light hydrocarbons include light aromatic hydrocarbons.
Exemplary light aromatic hydrocarbons include benzene, and toluene.

[0039] In some embodiments, for example, the solvent 106 is a supercritical fluid at the operating conditions of the contacting zone 103.

[0040] In some embodiments, the operating temperature in the solvent contacting zone is from between about the ambient temperature to about the critical condition of the solvent. In some embodiments, economics will determine the temperature range, even if, theoretically, it may be possible to operate in a significantly wider range. In some embodiments, the upper and lower ends of the operating temperature range is calculated as follows:

[0041] Tmax=Tc -0.05 (T-T0); and

[0042] T10w=Tc-0.80 (1-0-T0).

[0043] In some embodiments, the operating temperature is between about 80 C and about 200 C, such as between about 100 C and about 160 C.

[0044] In some embodiments, the asphaltenes 104a found in the feed 104 are insoluble in the solvent 106. The contacting of the solvent 106 and the feed 104 causes the asphaltenes 104a found in the feed 104 to precipitate into the asphaltene-rich material fraction 110 while the remainder of the feed 104 is solvated by the solvent 106 to form the deasphalted oil-comprising material fraction 108.

[0045] In some embodiments, for example, the separation in separation zone 109 is effected by gravity separation. In some embodiments, for example, the separation is effected by phase separation. In some embodiments, for example, the separation is effected by extraction.

[0046] In some embodiments, the asphaltene-rich material fraction 110, being denser than the deasphalted oil material fraction 108, is recovered as a bottoms product, and the deasphalted oil material fraction is recovered as an overhead product.

[0047] In some of embodiments, for example, both of the contacting zone 103 and the separation zone 109 is effected within a combined contactor/separator, such as a mixer-decanter or in an extraction column. In this respect, the contacting zone 103 and the separation zone 109 are at least partially co-located. Examples of suitable mixers include rotary stirring blades, paddles, or baffles.

[0048] In other embodiments, for example, the deasphalter 101 includes a mixer 103a, the contacting zone 103 defined by the mixer, and the resulting mixture 107 is then supplied to a separator, the separation zone 109 defined by the separator, to effect the gravity separation. In this respect, the contacting zone 103 and the separation zone 109 are separate.

[0049] In some embodiments, the deasphalted oil-comprising material fraction 108 includes substantially all of the solvent 106 and a partially de-asphalted oil, and the asphaltene-rich material fraction 110 includes a pitch and residual solvent.

[0050] In some embodiments, the de-asphalting process is characterized by the following operating parameters:
1. an operating temperature of the contacting;
2. the composition of the feed;
3. the composition of the solvent;
4. a ratio of the mass of the solvent to the mass of the feed ("S/F
ratio"); and 5. a ratio of the mass of the precipitated asphaltenes to the mass of the asphaltenes in the feed ("degree of asphaltene separation").

[0051] For example, the operating parameters will affect the properties of the S+PDA0 phase at operating conditions. The RI of the S+PDA0 phase can be measured, calculated, or both. In some embodiments, four operating parameters are specified, and a selected operating parameter is controlled based on the RI of the S+PDA0 phase.

[0052] In some embodiments, using the specified operating parameters, the RI of the S+PDA0 phase is calculated by two methods. In such embodiments, the selected operating parameter is controlled where the RI values of the S+PDA0 phase calculated using the two methods converge. In some embodiments, the selected operating parameter is controlled by obtaining a measured RI of the S+PDA0 phase and using at least one of the two calculation methods.

[0053]
A first method ("Method 1") for calculating the RI of the S+PDA0 uses the following equations:
114 Fitch Ris+PDA0 @T C = RIS+PDA00 @TT -F slope x A,a phaltenes (1) ¨Feed where:
RI S+PDA00 @T C = Ao + (A1 x RI
Feed @T C + A2 X RISolvent @T C) X UOP- ICSAolvent (2) slope = A4 + (A5 X RIFõd @Toc + A6 X RI
Solvent @T C) x UOP- KsA071vent (3) In these equations:
RIS+PDAO @TT: RI of the S+PDA0 at an operating temperature;
R1S+PDA00 @TT: RI of the S+PDA0 at the onset of precipitation at the operating temperature;
M Pitch: mass of the pitch;
Masphaltenes . mass of the asphaltenes in the feed composition;
Feed RIFeed @TY: RI of the feed at the operating temperature;
RISolvent @TT: RI of the solvent at the operating temperature;
( -1 19" KSolvent UOP-K characterization factor of the solvent; and A0-A7 coefficients determined experimentally through data analysis.

[0054]
The values of A0-A7 can be determined by fitting data obtained from experimental results. Alternatively or additionally, the values of A0-A7 can be determined by calculating RI's of various feeds, solvents and S+PDA0s, and also the UOP-K factors of various solvents.

[0055]
A hydrocarbon, such as a cut the feed 104 or a component of the solvent 106, can be characterized by its RI. Buckingham, "The Molecular Refraction of an Imperfect Gas"
(1956) 52 Transactions of the Faraday Society 747, showed that there is a correlation between RI and density:
Ri@rc2-1 x P@TY-1 = A + 1 3 X pwroc - F C X p@rc2 (4) Rl@Toc2 +2 where:
RI@T.c: RI of a compound at temperature T ( C);
Pgroc: density of the compound at temperature T ( C); and A, B, C: virial coefficients. Using data for a variety of hydrocompounds, the coefficients can be determined using curve fitting and data analysis.

[0056] The hydrocarbon can be further characterized by FRI, a function of its RI:
Ri@Toc2-1 FRI = RI@Toc2+2= P@T C(A + B X p@Toc + C X p@Toc2) (5)

[0057] JS Buckley et al, "Asphaltene Precipitation and Solvent Properties of Crude Oils", (1998) 16:3-4 Petrol Sci and Tech 251 showed that at ambient conditions and ideal volume of mixing, the FRI of a mixture can be calculated based on its components as follows:
Ei(vi @25oc)<1'ni @25-c) (6) FRI @25 C =
EiVi@25 C
where:
vi @25 C: volume fraction of component i in the mixture at 25 C; and FRI,i @25 C: FRI of component i in the mixture at 25 C.

[0058] FM Vargas and WG Chapman, "Application of the One-Third Rules in Hydrocarbon and Crude Oil Systems", (2010) 290:1 Fluid Phase Equilibria 103 showed a formula for extrapolating the RI of a hydrocarbon at a temperature T, based on the RI and density of the hydrocarbon at a reference temperature and the density of the hydrocarbon at the temperature T:
Ri@Toc2-1 = fu@T0oc2-1 x P@T C (7) Ri@Toc2 +2 RigT0T2 +2 P@To C

[0059] A hydrocarbon, such as a light hydrocarbon, can be characterized by a UOP-K
characterization factor. The UOP-K characterization factor can be calculated using the method set out in KM Watson and EF Nelson, "Improved Methods for Approximating Critical and Thermal Properties of Petroleum Fractions", 1933 85th Meeting of the American Chemical Society: Symposium on Physical Properties of Hydrocarbon Mixtures:
31,113PX 14 .8+92 UOP-K = n (8) ,@1.5.60c where:
UOP-K: UOP-K characterization factor of the hydrocarbon compound;
BP: boiling point of the hydrocarbon compound; and P@15.6.c: density of the hydrocarbon compound at 15.6 C.

[0060] In embodiments where the solvent 106 includes more than one hydrocarbon, the UOP-K characterization of the solvent can be calculated as a weighted aggregate of the UOP-K
characterization factor of each hydrocarbon according to:
UOP-K = Ei(wi x U0P-K1) (9) where:
w,: mass fraction of hydrocarbon, i, in the solvent; and UOP-K,: UOP-K characterization factor of the hydrocarbon.

[0061] A second method for calculating the RI of the S+PDA0 at the operating temperature uses mass balances and the correlations described in equations (4)-(7) ("Method 2").

[0062] In embodiments where RI is calculated using Method 1 and Method 2, an initial value is specified for the selected operating parameter. The initial value is used to calculate the RI of the S+PDA0 at the operating temperature using Method 2. The convergence of the RI of the S+PDA0 at the operating temperature calculated using Method 1 and Method 2 indicates that the value of the selected operating parameter used in the calculation of Method 2 is the value that should be used in the solvent de-asphalting process. If the values of the RI of the S+PDA0 at the operating temperature calculated using Method 1 and Method 2 do not converge, a new value of the selected operating parameter is specified and the RI of the S+PDA0 at the operating temperature is re-calculated using Method 2. This calculation can be iterated with new values of the selected operating parameter until the values RI of the S+PDA0 at the operating temperature calculated using Method 1 and Method 2 converge.

[0063] In some embodiments, the de-asphalting system 100 includes a flow regulator 114 operatively connected to the controller 112 for controlling a flow feed rate of the feed 104, a solvent feed rate of the solvent 106, or both.

[0064] In some embodiments, the de-asphalting system 100 includes a temperature regulator 116 operatively connected to the controller 112 for controlling the operating temperature. In some embodiments, the temperature regulator is a heater 111.
Examples of suitable heaters include heat exchangers, furnaces, or boilers.

[0065] In some embodiments, the de-asphalting system 100 includes a pre-heater (not shown) upstream of the deasphalter 101 for pre-heating the feed 104, the solvent 106 or both.

[0066] In some embodiments, the de-asphalting system 100 includes an RI
determining device 117 operatively connected to the controller 112 for determining the RI
of the S+PDAO
108. In some embodiments, the RI determining device is a refractometer for measuring the RI of the S+PDAO 108. In some embodiments, the RI determining device is a densitometer for measuring the density of the S+PDAO to determine the RI of the S+PDAO, for example, by using the correlation set out in equation (4).

[0067] In some embodiments, the de-asphalting system 100 includes a secondary de-asphalter (not shown) for removing at least a portion of the asphaltenes present in the S+PDAO
phase 108.

[0068] In some embodiments, the de-asphalting system 100 includes a S+PDAO
separator (not shown) for separating the S+PDAO 108 to obtain a S+PDAO-derived solvent. In such embodiments, the solvent 106 includes at least a portion of the S+PDAO-derived solvent.

[0069] In some embodiments, the de-asphalting system 100 includes a pitch stripper (not shown) for separating the asphaltene-rich material fraction 110 to obtain a pitch-derived solvent. In such embodiments, the solvent 106 comprises at least a portion of the pitch-derived solvent.

[0070] In another aspect, there is provided a method for solvent deaspalting 200 (Figure 2). At block 202, a feed, including asphaltenes, at a feed flow rate is provided. At block 204, a solvent at a solvent flow rate is provided. At block 206, the feed and the solvent are contacted to effect precipitation of at least a portion of the asphaltenes to obtain a S+PDAO and an asphaltene-rich material fraction. The asphaltene-rich material fraction, includes the precipitated asphaltenes. The contacting is disposed of at an operating temperature. At block 208, at least one operating parameter is controlled based on at least a refractive index of the S+PDAO, the operating parameter is selected from: the operating temperature; the composition of the feed;
the composition of the solvent; a ratio of the precipitated asphaltenes to the mass of asphaltenes within the feed; and a ratio of the feed flow rate to the solvent flow rate.

[0071] In another aspect, there is provided a deasphalted oil obtained by a method 300 (Figure 3). At block 302, a feed, including asphaltenes, at a feed flow rate is provided. At block 304, a solvent at a solvent flow rate is provided. At block 306, the feed and the solvent are contacted to effect precipitation of at least a portion of the asphaltenes to obtain a S+PDAO and an asphaltene-rich material fraction. The asphaltene-rich material fraction, includes the precipitated asphaltenes. The contacting is disposed of at an operating temperature. At block 308, at least one operating parameter is controlled based on at least a refractive index of the S+PDAO, the operating parameter is selected from: the operating temperature;
the composition of the feed; the composition of the solvent; a ratio of the precipitated asphaltenes to the mass of asphaltenes within the feed; and a ratio of the feed flow rate to the solvent flow rate.

[0072] In another aspect, there is provided a method for solvent de-asphalting 400 (Figure 4). At block 402, operating parameters of the de-asphalting are defined, the operating parameters including: a composition of a feed, including asphaltenes; a target ratio of a mass of removed asphaltenes to the mass of asphaltenes within the feed; an operating temperature for contacting the feed and a solvent; and a ratio of a feed flow rate of the feed to a solvent flow rate of the solvent. At block 404, an RI of the solvent is determined based at least on calculating the RI of an S+PDA0 formed by contacting the feed with the solvent. At block 406, a solvent is selected based at least on the solvent RI determined at block 404. At block 408, the solvent selected in block 406 is contacted with the feed at the operating parameters defined at block 402 to effect de-asphalting.

[0073] In another aspect, there is provided a method for solvent de-asphalting 500 (Figure 5). At block 502, a solvent is selected based on RI. At block 504, the selected solvent is contacted with a feed including asphaltenes to effect de-asphalting.

[0074] In another aspect, there is provided a method for starting up a solvent deasphalting process 600 (Figure 6). At block 602, four operating parameters are set at pre-determined values, the operating parameters are selected from: an operating temperature; a composition of a feed; a composition of a solvent; a target ratio of a mass of precipitated asphaltenes to a mass of asphaltenes initially within the feed; and a ratio of a feed flow rate to a solvent flow rate. At block 604, the non-predetermined operating parameter is determined based on an expected RI of an S+PDA0 stream generated by the process. At block 606, the process is started up using the pre-determined operating parameters and the determined operating parameter.

[0075] Other features and embodiments of the invention will become apparent from the following examples which are given for illustration of the invention rather than for limiting its intended scope.

Examples

[0076] In the following illustrative examples, a S/F ratio for a solvent de-asphalting process is controlled.
Example 1: Defining Process variables

[0077] In this example, the S/F ratio is controlled at a first stage de-asphalting operation.

[0078] The following four operating parameters are selected:
1. the operating temperature;
2. the feed composition;
3. the solvent composition; and 4. the degree of asphaltene separation.

[0079] 1) Temperature: In this example, the operating temperature is 165 C.

[0080] 2) Feed composition:

[0081] In this example, the feed composition is bitumen. Bitumen is a mixture of components and can be characterized as having five fractions (or "cuts"): a kerosene fraction, a diesel fraction, a light vacuum gas oil fraction, a heavy vacuum gas oil fraction, and a vacuum residue fraction.

[0082] In this example, the bitumen has the following composition:
Table 1: Feed composition Initial Final Volume Density Density Density Boiling Weight fraction @ @
Cut Boiling @ 25 C
Point fraction @
Point (C) 25 C (kg/m (.C) 15.6 C3 (4/M3) ) (kg/m3) Kerosene 190 260 0.0215 0.0252 869.88 Diesel 260 343 0.0589 0.0669 899.99 Light Vacuum 343 454 0.1693 0.1844 937.64 Gas Oil Heavy 454 560 0.1776 0.1851 979.38 Vacuum Gas Oil Vacuum 560 820 0.5727 0.5384 1,086.01 Residue Total 190 820 1.0000 1.0000 1,027.60 1,021.03 932.45 (Bitumen)

[0083] The bitumen of this example includes asphaltene having the following properties:
Table 2:
Initial Final Volume Density . Density Density g @
Component Boiling Boiling Weight fraction Point fraction g 15.6 C 11 2,5 Cµ 165 C
Point ( C) (,,C) 25 C (kg/m3) vµgirri3i (kg/m3) C5-asphaltenes - - 0.1948 0.1655 1,210.00 1,201.93 1,119.30

[0084] 3) Solvent composition:

[0085] The solvent can be one or more solvents. In this example, the solvent has the following composition:
Table 3: Solvent composition Carbon Weight Volume fraction Density g 15.6 Boiling Component No. fraction @ 25 C C (kg/m3) Point ( C) Paraffins 0.9585 0.9583 Propane C3 0.0002 0.0002 507.0 -42 lso Butane i-C4 0.0003 0.0004 562.9 -12 Normal Butane n-C4 0.1027 0.1120 584.0 -1 !so Pentane i-05 0.5652 0.5748 624.7 28 Normal Pentane n-05 0.1673 0.1684 631.1 36 Normal Hexane C6 0.0490 0.0468 663.8 69 Heptanes C7 0.0248 0.0228 688.2 98 Octanes C8 0.0135 0.0120 707.0 126 Nonanes+ C9+ 0.0243 0.0209 734.2 174 Naphthenes 0.0346 0.0288 Cyclopentane & & 0.0160 0.0136 750.4 49 Methylcyclopentane Cyclohexane & & 0.0186 0.0152 783.5 81 Methylcyclohexane Aromatics 0.0179 0.0129 Benzene C6H6 0.0044 0.0031 882.9 80 Aromatics C7+ C7+ 0.0135 0.0098 874.3 111 Note:
`Nonanes+' density/boiling point were approximated with Decane density/boiling point.
`Cyclopentane & Methylcyclopentane' density/boiling point were approximated with Cyclopentane density/boiling point.
`Cyclohexane & Methylcyclohexane' density/boiling point were approximated with Cyclohexane density/boiling point.
'Aromatics C7+' density/boiling point were approximated with Toluene density/boiling point.

[0086] In this example, the solvent has the following properties:

[0087] Table 4: Solvent density Property Unit Value Density @ 15.6 C kg/m3 635.15 Density @ 25 C kg/m3 625.47 Density @ 165 C kg/m3 447.61

[0088] 4) The degree of asphaltene separation:

[0089] In this example, the degree of asphaltene separation is 50%, i.e.
half of the asphaltenes of the bitumen will be precipitated. Asphaltenes are those compounds that are not soluble in solvent. It is assumed that these are the only insoluble compounds in the feed. As such, it is assumed that the pitch will consist only of asphaltenes.

Example 2: Calculating Rls+pDAo@rc using developed equations:

[0090] As noted above, the RI of the S+PDA0 can be calculated using Method 1 with the following equations:
MPitch RIS+PDA0 @T C m ¨asphaltenes (1) = RIS+PDA00 @T C + slope x cs '"Feed where:
RI S+PDA00 @T C --= Ao -I- (A1 x RI
Feed @T C + A2 x RISolvent @T C) X U OP -KSA:lvent (2) slope = A4 + (A5 x RI
Feed @T C 4- A6 x RISolvent @T C) x "P-KSA:lvent (3)

[0091] The values of A0-A7 are determined by fitting data obtained from experimental results.

[0092] First, the RI of the feed and solvent at the operating temperature are calculated (see Ex 2.1 and 2.2, below)

[0093] Second, the RI of the S+PDA0 at the extraction temperature (Rlstage S+PDA0 @T C) is calculated literature correlations (see Ex 3.3, below)

[0094] Third, the RI of the S+PDA0 at the extraction temperature (Rlstage S+PDA0 @T C) is calculated using experimental results (see Ex 2.4)

[0095] Lastly, the coefficients Ao ¨ A7 are tuned to minimize the difference between the RI of the S+PDA0 at the extraction temperature calculated in the second and third steps.

[0096] Using this method, it is determined that there are three possible sets of values for A0¨A7: 1) a first stage de-asphalting operation operating at temperatures >120 C; 2) a first stage de-asphalting operation operating at temperatures <100 C; and 3) a second stage de-asphalting operation as set out below:

[0097] Table 5.
Stace 1 High T (>120 C) Low T (<100 C)_ Stage 2 AO= 0.14953 0.14953 0.04430 Al = -0.02996 -0.02996 0.02534 A2 = 0.29936 0.29936 0.94565 A3 = 0.50000 0.50000 0.00000 A4 = -0.34939 -0.34908 -0.00699 A5= 474.775 0.51249 0.00000 A6= -419.986 -0.38067 0.00000 A7 = -2.50000 0.00000 0.00000

[0098] Based on equations (1)-(3), it is seen that RI Feed @T C) RISolvent @T C)UOP ¨
KSolvent are determined before solving for RI
S+PDA0 @T C = These are calculated in Examples 2.1, 2.2 and 2.3, respectively. The RIS+PDA0 @T C is calculated in Example 2.4.
Example 2.1: Calculate RI Feed @T C
Example 2.1.1: Calculate RI of each component fractions of the feed

[0099] Recall equation (4) above:
Ri@T0,2-1 2 X pgroC A B X P@ToC C X P@ToC2 (4) R/grc +2

[00100] The virial coefficients, A, B and C, are determined using fitting and data analysis for a variety of hydrocarbon compounds. These are determined to be 0.4597, -0.2425, and 0.1134, respectively.

[00101] Equation (4) is modified to solve for RI with a known density:
(10) 2 x (0.4597 xP70207 0.2425x(P702050n2+0.1134x(P70205:93)+1 RI@25 C
1¨ (0.4597 xP@25'c 0.2425492 +0.1134x(P@25 93 Imo l000 l000

[00102] Equation (10) is used to calculate the RI of each cut:
(10a) ito@or C)2ito@ 93)+
o0 2 x (0.4597 xPcut@25000 c 0.2425x(PCU
l +0.1134x(PCU25 RICut @25 C =
1¨ (0.4597 xPcult0:025 C-0.2425x (PCulto@o025 92 + 0.1134X (PCUt @25C)3

[00103] The results are shown below (densities from Table 1, above):
Boiling Point Cut Density @ 25 C (kg/m3) RI
--cut @noc Kerosene 869.88 1.4938 Diesel 899.99 1.5118 Light Vacuum Gas Oil 937.64 1.5350 Heavy Vacuum Gas Oil 979.38 1.5617 Vacuum Residue 1,086.01 1.6378 Example 2.1.2: Calculate FRI, a function refractive index, for each cut

[00104] Recall equation (5), above:
_ RI@Toc2-1 FRI = pgroc(A B X p@Toc C X p@Toc2) (5) RI@Toc+2

[00105] Equation (5) is modified to calculate the FRI of each fraction:
RILt @25 C-1 (5a) FRI,Cut @25 C ¨ 2 RICUt @25 C +2

[00106] The results are shown below (densities from Table 1, above):
Boiling Point Cut Density @ 25 C (kg/m3) RI
-- cut @25 C FRI,Cut @25 C
Kerosene 869.88 1.4938 0.2910 Diesel 899.99 1.5118 0.3000 Light Vacuum Gas 937.64 1.5350 0.3113 Oil Heavy Vacuum 979.38 1.5617 0.3241 Gas Oil Vacuum Residue 1,086.01 1.6378 0.3593 Example 2.1.3: Calculate FRI for the entire feed:

[00107] Recall equation (6), above:
Ei(vi @2soc) (6) FRI @25 C =
L4 't @25.c

[00108] Equation (6) is used to calculate the FRI of the feed composition:
Ei(vcuti @25 C X FRI,Cuti @25 C) FRI Feed @25 C = (6a) Li VCuti @25 C

[00109] Recall:

Boiling Point Cut FRI,Cut @25 C Volume fraction @ 25 C
Kerosene 0.2910 0.0252 Diesel 0.3000 0.0669 Light Vacuum Gas Oil 0.3113 0.1844 Heavy Vacuum Gas Oil 0.3241 0.1851 Vacuum Residue 0.3593 0.5384 Note: Volume fractions from Table 1

[00110] Solving for FRI, Feed @ 25 C:
Ei(vcuti @2s0cxFR1,cut1 @25 C) FRI,Feed @25 C =
Ei vCuti @25 C
V kerosene @125 CXF RI,kerosene @25T+V diesel @25 C XFRI,diesel @25T+VLVG0 @25 CXFRI,LVG0 @25 C
FRI,Feed @25 C
V kerosene @25 C+V diesel @25 C+vly co @250c+vHvco @25 c+vvR @25 C
VHVGO @25 CXFRI,HVG0 @25 C+VVR @250C)<FRI,VR @25 C
FRI,Feed @25 C ,kerosene @250C+V diesel @25 C+V LV GO @25 C+V HV GO @,25 c+vvR @25 C
0.00252 x0.2910+0.00669x0.3000+0.1844X0.3113+0.1851x0.3241+0.5384x0.3593 FRI,Feed @25 C 0.00252+0.00669+0.1844+0.1851+0.5384 FRI,Feed @25 C = 0.3382 Example 2.1.4: Calculate RI for the entire feed:

[00111] Recall equation (5):
in@Toc 2 ¨1 FRI = = p@Toc (A + B x p@Toc + C x p@m2) (5) 1710,o,- +2

[00112] Equation (5) is re-arranged to solve for the RI:
Ri@Toc = _______________________________________________________________ (11)

[00113] Equation (11) can be used to solve for the RI of the Feed @ 25 C:
,Feed RIFeed @25 C = 2XF RI @250-1 (11a) FRI,Feed @25 C
Where FRI Feed @25 C = 0.3382 (Ex 2.1.3)

[00114] Solving for RIFeed @ 25 C:
2X FRI ,Feed @25 C + 1 2 x 0.3382 + 1 RI Feed @25 C = ___________________________ = 1.5917 1 FRI,Feed @25 C 1 ¨ 0.3382 Example 2.1.5 Calculate RI at the operating temperature:

[00115] Recall equation (7):
Ri@pc2-1 = Ri@T0.,2-1 x P@T C (7) Ri@rc2 +2 Ri@Tec2 +2 P@To C

[00116] Equation (7) is rearranged to solve for the RI of a new temperature given a reference temperature of 25 C:
(12) c.
+ 1 2X 2 p@To RI@25 C+2 P@25 C
Ri@Toc = 0,2 @,25 C-1 P@rc 1 , R%2+2 P@25 C

[00117] Recall (from Table 1):
Boiling Point Cut Density @ 25 C (kg/m3) Density @ 165 C (kg/m3) Total (Bitumen) 1,021.03 932.45

[00118] Solving for RI of the feed at the operating temperature:
RiTeec, @25.c-i_xPFeed @i65-c+i 2x 2 1.59172-1 932.46 õ X + 1 Feed @25 C+2 PFeed @25 C 2X1.5917- +2 1021.03 RIFeed @165 C = 1.5300 RI F2 eed @25 C-1 PFeed @165 C 1-1'59172-1 932.46 , X
1 ¨ X
RI F2 eed @250c+2 P Feed @,25 C 1.5917-.42 1021.03 Example 2.2: Calculate RISolvent @T C (using same method as the feed):

[00119] RIS @165 C 7-- 1.2477 Example 2.3: Calculate U0P-Ksovent Example 2.3.1: Calculate UOP-K for each component in the solvent:

[00120] Recall equation (8):
3.1BPx 1.8+ 492 UOP-K = P@15 6 C (8)

[00121] Solving for each component of the solvent (using density and boiling point from Table 3, above):
Component Carbon No. Boiling Point ( C) Density @ 15.6 C (kg/m3) U0P-K1 Paraffins Propane C3 -42 507.0 14.73 Is Butane i-C4 -12 562.9 13.82 Normal Butane n-C4 -1 584.0 13.51 Iso Pentane i-05 28 624.7 13.05 Normal Pentane n-05 36 631.1 13.04 Normal Hexane C6 69 663.8 12.82 Heptanes C7 98 688.2 12.71 Octanes C8 126 707.0 12.67 Nonanes+ C9+ 174 734.2 12.67 Naphthenes Cyclopentane & C5H10 &
49 750.4 11.11 Methylcyclopentane C6H12 Cyclohexane & C6H12 &
81 783.5 10.98 Methylcyclohexane C7H14 Aromatics Benzene C6H6 80 882.9 9.74 Aromatics C7+ C7+ 111 874.3 10.11 Example 2.3.2: Calculate UOP-K for the combined solvent

[00122] Recall equation (9) UOP-K = Ej(wi x U0P-K1) (9)

[00123] Using the weight fractions from Table 2 and the UOP-K's calculated in the previous step:
U0P-Ksoivent Ei( W x UOP-K) =
"13-KSolvent = (W3 X U0P-Ko Wic4 X U0P-K1c4 -= wAromatics C7+ X UOP-KAromatics C7+
U0P-ICSolvent = (0.0002 x 14.73 + 0.0003 x 13.82 + === + 0.0135 x 10.11 =
OP-KSolvent 12.94 Example 2.4: Calculate RI of the S+PDA0 at 165 C using Method 1:

[00124] Recall:
The degree of asphaltene separation is selected to be 0.5 (i.e. Ancs masPgcaitenes = 0.5) (Ex. 1) '"Feed The values of A0-A7 are found in Table 1, using the values for stage 1 and temperatures of above 120 C.
The values of RIFeed, Rlsoivent, and U0P-Ks01vent were calculated above (Ex 2.1, 2.2, and 2.3)

[00125] Example 2.4.1 calculate RIS+PDA00@l65 C

[00126] Solve for RIS+PDA00@1.65 C using equation (2):
RIS+PDA00@l65 C = Ao (A1 X RIFeed @165 C A2 X RISolvent @165 C) X U0P-KSAolvent (2) RIS+PDA00@l65 C = 0.14953 + (-0.02996 x 1.5300 + 0.299936 x 1.2477) x 12.94 '5 RIS+PDA0c0165 C = 1.3281 Example 2.4.2 calculate slope

[00127] Solve for slope using equation (3) slope = A4 + (A5 X RI
Feed @165 C + A6 X RISolvent @165 C) X U0P-KSAolvent (3) slope = ¨0.34939 + (474.775 x 1.5300 ¨ 419.986 x 1.2477) x 12.9425 slope = ¨0.0133 Example 2.4.2 calculate RI S+PDA0@l65 C

[00128] Solve for RI
S+PDA0@l65 C7 using equation (1):
MPitch (1) RIS+PDA0@l65 C RIS+PDA00@1.65 C + slope x õC5-asphaltenes '"Feed RIS+PDA0@l65 C = 1.3281 ¨ 0.0133 x 0.5 RIS+PDA0@l65 C = 1.3215 Example 3: Calculating Ris+pDA0 using correlations from the literature and mass balances.

[00129] The RIS+PDA0 is calculated using correlations from the literature and mass balances (Method 2). This calculated value will be compared to the Rls+pDA0 calculated in Ex 2 using Method 1. The convergence of these values is used to control the S/F
ratio (Ex 4).

[00130] Equation (12) is re-arranged to solve for RI of the S+PDAO:

RIL-PDAO @25 C-1X PS+PDA0 @T C +1 RI S+PDA0 @25 C+2 PS+PDA0 @25 C (12b) RIS+PDA0 @T C Riz S+PDA0 @25 C-1 PS+PDA0 wrc RI S+PDA0 @25 C+2 PS+RDAo @zs*c

[00131] The values of io S+PDA0 @25 C, PS+PDA0 @TY and RIS+PDA0 @25 C are calculated first (Ex 3.2, 3.3) before calculating RI
S+PDA0 @TY (Ex 3.3).
Example 3.1 Guess the S/F ratio:

[00132] The S/F ratio is the operational parameter being controlled (see Ex 1). This value will affect the equilibrium of the streams (e.g. the densities of the pitch and S+PDA0 will be affected).

[00133] Start with an initial guess for the S/F ratio. In this example, the initial guess is:
S/F=1.20 Where S/F: S/F Ratio (on weight basis).
Example 3.1.1 Calculate the weight % (on Feed basis) of Solvent:

[00134] By applying a mass balance:
WSolvent = WFeed X (S/F) (13) Where:
wsolvent: Weight % (on Feed basis) of Solvent;
ti/Feed: Weight % (on Feed basis) of Feed (i.e. 100, by definition);
and S/F: Solvent to Feed Ratio (on weight basis).

[00135] Solving:
wSolvent wFeed X (S/F) = 100 * 1.20 = 120 wt%
Example 3.2 Calculate o ,S+PDA0 @25 C, PS+PDA0 @T C
Example 3.2.1 Calculate the density of the pitch:

[00136] Recall from Ex. 1, that the pitch consists of C5-asphaltenes. It follows that the density of the pitch is equal to the density of the C5-asphaltenes:
PPitch @T C = PC5-asphaltenes @T C
(14)

[00137] Recall from Table 2:
Component Density @ 15.6 C (kg/m3) Density @ 25 C (kg/m3) Density @ 165 C
(kg/m3) C5-asphaltenes 1,210.00 1,201.93 1,119.30 Example 3.2.2 Calculate the weight % (on Feed basis) of Pitch:

[00138] Since the pitch is the portion of the 05-asphaltenes removed from the feed:
C5-asphaltenes MpLtch wPitch WFeed X cs-asphaltenes MFeed (15) Where:
wPitch: Weight % (on Feed basis) of Pitch after phase separation has occurred;
wFCe5e-da5phaitene5: Weight % (on Feed basis) of C5-asphaltenes in the Feed.
(Table 1);
M Pitch: Mass of pitch after phase separation has occurred; and m FC e5 e-dasphaltenes : Mass of C5-asphaltenes in the Feed.

[00139] Solving for Wpitch:
wPitch = C5-aspha1ten mCs¨asphaltenes es MPitch = 19.48 X 0.5 = 9.74 wt%
W Feed x Feed

[00140] Since the partially de-asphalted oil will be the portion of the feed after the removal of the pitch:
WPDAO = wFeed wPitch (16) Where wpDA0: Weight % (on Feed basis) of partially de-asphalted oil after phase separation has occurred;
wFeed: Weight % (on Feed basis) of Feed (i.e. 100, by definition); and W pitch: Weight % (on Feed basis) of Pitch after phase separation has occurred (Ex 3.2.2).

[00141] Solving:
WPDAO = wFeed wPitch 100 ¨ 9.74 = 90.26 wt%
Example 3.2.4 Calculate the density of the PDAO:

[00142] The density of the partially de-asphalted oil can be calculated as follows:
WPDAO
(17) PPDAO wrc wFeed w Pitch PFeed @T C PP itch wrc Where PPDAO @VC: Density of the partially de-asphalted oil at a specified temperature, after phase separation has occurred, in kg/m3;
WPDAO: Weight % (on Feed basis) of partially de-asphalted oil, after phase separation has occurred (Ex. 3.2.3);
WFeed: Weight % (on Feed basis) of the Feed (i.e. 100, by definition);
PFeed @TT: Density of the Feed at a specified temperature, in kg/m3 (Table 1);
wPitch: Weight % (on Feed basis) of the Pitch, after phase separation has occurred (Ex 3.2.2); and Ppitch wrc: Density of the Pitch at a specified temperature, after phase separation has occurred, in kg/m3 (Ex. 3.2.1).

[00143] Solving for density at 25 C and operating temperature (165 C):
WPDAO 90.26 kg PPDAO @25 C = w Feed w Pitch = 100 9.74 = 1,004.72 PFeed @25 C P Pitch @23 C 1021.04 1,201.93 WPDAO 90.26 kg PPDAO @165 C = w Feed wPitch 100 9.74 = 915.96 ¨3-PFeed @165 C PPitch@l65 C 932.46 1,119.30 Example 3.2.5 Calculating the weight of the solvent in the pitch+solvent phase

[00144] Based on experimental data, the weight fraction of solvent in the Pitch+Solvent, after phase separation is determined to be correlated with the density of pitch at the extraction temperature according to the following formula:

wmcvcst , _1.29195 x (Pp t1tc070 ) + 1.86145 (18) Where:
õ,pitch+s= Solvent.
w weight fraction of solvent in the Pitch+Solvent, after phase separation has occurred; and ppitch@ Toc: density of pitch at the extraction temperature, in kg/m3 (Ex 3.2.1).

[00145] Solving for wi,siticyCst:
,,Solvent "Pitch+s ¨ ¨1.29195 X PPitch@ 165 C + 1.86145 1Vch-s Solvent = ¨1.29195 x (1.11930) + 1.86145 Solvent 41.54 wt%
wPitch+s ¨
Example 3.2.6 the weight % (on Feed basis) of Pitch+S:

[00146] By applying a mass balance:
wPitch (19) wPitch+S = 100 ¨ Solvent W
Pach+s Where wPitch+S: Weight % (on Feed basis) of pitch-solvent;
wPitch: Weight % (on Feed basis) of Pitch (Example 3.2.4); and ,,Solvent. Pitch+s = Weight % (on Pitch+S basis) of Solvent in pitch-solvent (Ex. 3.2.5).
"

[00147] Solving:
WPitch 9.74 = 16.66 wt%
wpitch+s = 100¨wSolvent ¨ 1-41.54 ¨ Pitch+S
Example 3.2.7 calculate the density of the Pitch+Solvent:

[00148] The density of the pitch-solvent can be calculated as follows:
WPitch+S
(20) PPitch+S @25 C = wPitch+S¨wPitch+ wPitch Ps @25 C PPitch@25 C
Where PPitch+S @25 C: Density of the pitch-solvent at 25 C, after phase separation has occurred, in kg/m3;
wPitch+S: Weight % (on Feed basis) of pitch-solvent after phase separation has occurred (Ex 3.2.6);
wPitch: Weight % (on Feed basis) of Pitch, after phase separation has occurred (Ex 3.2.2);
Ps @25 C: Density of the Solvent at 25 C, in kg/m3 (Table 4); and PPitch@25 C: Density of the Pitch at 25 C, after phase separation has occurred, in kg/m3 (Ex 3.2.1).

[00149] Solving:
WPitch+S 16.66 , kg PPitch+S @25 C = wPitch+s¨wPitch+ wPitch = 16.66-9.74+ 9.74 Ps @,25 c PPitch @25 C 625.47 1,201.93 Example 3.2.8 Calculate the weight A (on Feed basis) of the S+PDAO:
The weight of the S+PDAO phase can be calculated by a mass balance:
wS+PDA0 = wFeed wSolvent wPitch+S (21) Where WS+PDAO: Weight % (on Feed basis) of S+PDAO, after phase separation has occurred;
wFeed: Weight % (on Feed basis) of Feed (i.e. 100, by definition);
wsoivent : Weight % (on Feed basis) of Solvent (Ex 3.1.1); and Wpitch+s : Weight % (on Feed basis) of pitch-solvent, after phase separation has occurred (Ex. 3.2.6).

[00150] Solving:
wS+PDA0 = wFeed wSolvent wPitch+S = 100 + 120 ¨ 16.66 wS+PDA0 = 203.33 wt%
Example 3.2.9 Calculate the density of the S+PDAO at 25 C and at the extraction temperature:
The density of the S+PDAO phase ws+PDA0 PS+PDA0 @VC = wS+PDAO¨wPDA0+ wPDA0 (22) Ps @T C PPDAO @T C
Where PS+PDA0 @T C: Density of the S+PDAO at the operating temperature in C, after phase separation has occurred, in kg/m3;
WS+PDAO: Weight % (on Feed basis) of S+PDAO after phase separation has occurred (Ex 3.2.8);
wPDAO: Weight % (on Feed basis) of partially de-asphalted oil after phase separation has occurred (Ex 3.2.3);
Ps grc: Density of the solvent at the specified temperature in C, in kg/m3 (Table 4); and PPDAO @T C: Density of the partially de-asphalted oil at the specified temperature in C, after phase separation has occurred, in kg/m3 (Ex 6.2.4).

[00151] Solving for density of the S+PDAO at a reference temperature and the operating temperature:
WS+PDA0 203.33 kg m3 PS+PDA0 @25 C = wS+PDAO¨wPDA0 wPDA0 = 203.33-90.26+ 90.26 = 751.37¨
PS @25 C PPDAO @25 C 625.47 1,004.72 WS+PDA0 203.33 .,2 kg PS+PDA0 @165 C = wS+PDAO¨wPDA0 wPDA0 = 203.33-90.26+ 90.26 = 57a 0m3 Ps @165 C PPDAO @165 C 447.61 915.96 Example 3.3 Calculate Ris+pDAo@Toc Example 3.3.1 the volume % of Pitch (on Feed basis) at 25 C:
wPitch*100 vPitch @25 C = wi F
PPitch@25 C*LAPi,F 25 C (23) Where VPitch @25 C: Volume % (on Feed basis) of Pitch at 25 C, after phase separation has occurred;
wPitch: Weight % (on Feed basis) of Pitch, after phase separation has occurred (Ex 3.2.2);
PPitch @25 C: Density of the Pitch at 25 C in kg/m3, after phase separation has occurred (Ex 3.2.1);
wi,F: Weight % (on Feed basis) of a Feed boiling point cut (Table 1); and Pi,F @ 25 C: Density of a Feed boiling point cut at 25 C, in kg/m3 (Table 1).

[00152] Solving:
Wi F = W190-260 C,F W260-343 C,F ______ W343_454 CF +
W454-560 C,F
õ
i,F @ 25 C P190-260 C,F @ 25 C P260-343 C,F @ 25 C P343-454 C,F @
25 C P454-560 C,F @ 25 C
W560-820 C,F
P560-820 C,F @25 C
E WiF 2.15 5.89 16.93 17.76 57.27 t, Pi,F @25 C 869.88 +'899.99 +'937.64 +'979.38 + 1086.01 ZI __________ = 0.0979 P i,F @25 C
wPitch*100 9.74*100 vPitch @25 C
PPitch @25C*Li __________________ 1,201.93*0.0979 = 8.27 vol /o PL
,F @ 25 C
Example 3.3.2 Calculate the volume % of Solvent (on Feed basis) at 25 C:

[00153] The volume of solvent can be calculated as follows:
W Solvent*100 vSolvent @25 C = w i F
Psolvent @2s c-z.,,iõ (24) i,F @ 25 C
Where vSolvent @25 C: Volume % (on Feed basis) of Solvent at 25 C, after phase separation has occurred;
wsozvent: Weight % (on Feed basis) of Solvent, after phase separation has occurred (Ex 3.1.1);
PSolvent @25 C: Density of the Solvent at 25 C, in kg/m3 (Table 3);
wi,F: Weight % (on Feed basis) of a Feed boiling point cut (Table 1); and Pi,F @ 25 C: Density of a Feed boiling point cut at 25 C, in kg/m3 (Table 1).

[00154] Recall, Z, wi'F = 0.0979 (Example 3.3.1).
Pi,F @ 25 C

[00155] Solving:
wSolvent*100 120*100 VSolvent @25 C = v F = 625.47*0.0979 = 195.88 vol0/0 PSolvent @25 C*Lt P i,F @ 25 C
Example 3.3.3 Calculate the volume % of Pitch+S (on Feed basis) at 25 C:

[00156] The volume of pitch-solvent can be calculated as follows:
wvitch+s*100 VPitch+S @25 C = v wi F
PPitch+S @250C*Z4 (25) ,i,F @ 25 C
Where VPitch+S @25 C: Volume % (on Feed basis) of pitch-solvent at 25 C, after phase separation has occurred;
WPitch+S: Weight % (on Feed basis) of pitch-solvent, after phase separation has occurred (Ex 3.2.6);
PPitch+S @25 C: Density of the pitch-solvent at 25 C, in kg/m3 (Ex 3.2.7);
wi,F: Weight % (on Feed basis) of a Feed boiling point cut (Table 1); and Pi,F @ 25 C: Density of a Feed boiling point cut at 25 C, in kg/m3 (Table 1).
Recall, Z, _________ = 0.0979 (Ex 3.3.1).
Pi,F @ 25 C

[00157] Solving:
wpitch+s*no 16.66*100 VPitch+S @25 C = v wi F = 869.19*0.0979 % 19.57 vol /o @25 C*La,-, @25 C
Example 3.3.4 the volume % of PDAO (on Feed basis) at 25 C:

[00158] The volume % of PDAO (on Feed basis) at 25 C is calculated via a mass balance:
VPDAO @25 C 'Feed @25 C V Pitch @25 C (26) Where V PDAO @25 C: Volume % (on Feed basis) of partially de-asphalted oil at 25 C, after phase separation has occurred.
VFeed @25 C: Volume % (on Feed basis) of Feed at 25 C (i.e. 100, by definition) VPitch @25 C: Volume % (on Feed basis) of Pitch at 25 C, after phase separation has occurred. (Ex 3.3.1)

[00159] Solving:

V PDAO @25 C = VFeed @25 C VPitch @25 C = 100 ¨ 8.27 = 91.72 vol%
Example 3.3.5 Calculate the volume A of S+PDA0 (on Feed basis) at 25 C:

[00160] The volume of S+PDA0 (on feed basis) at 25 C is calculated via a mass balance:
VS+PDA0 @25 C = VFeed @25 C VSolvent @25 C VPitch+S @25 C (27) Where:
VS+PDA0 @25 C: Volume % (on Feed basis) of solvent-partially de-asphalted oil at 25 C, after phase separation has occurred.
VFeed @25 C: Volume % (on Feed basis) of Feed at 25 C (i.e. 100, by definition) VSolvent @25 C: Volume % (on Feed basis) of Solvent at 25 C. (Ex 3.3.3) V Pitch+S @25 C: Volume A (on Feed basis) of pitch-solvent at 25 C, after phase separation has occurred. (Ex 3.3.4)

[00161] Solving:
Volume % of S+PDA0 (on Feed basis) at 25 C
VS+PDA0 @25 C VFeed @25 C VSolvent @25 C VPitch+S @25 C
VS+PDA0 @25 C = 100 + 195.88 ¨ 19.57 VS+PDA0 @25 C 276.31 vol%
Example 3.3.6 Calculate RI of pitch:

[00162] Equation (10) is used to calculate the RI of pitch @ 25 C:
cpiticonz25.93)+1 2 x (0.4597 xPPitch __________ @25'c 0.2425x(PPIticoho@o25 92+0.1134x noo RI Pitch @25 C (10b) 1¨ (0.4597 xPPitch @2S C 0.2425x (PPit1c0h07025 92+0.1134x(PPit1c0h0:25 93) woo Where:
RI itch @25 C: Refractive index of the Pitch at 25 C; and p pitch @25 C: Density of the Pitch at 25 C, in kg/m3. (Ex 3.2.1).

[00163] Solving:

_____________________________ 2 x (0.4597 xPPitch @ZST 0.2425x(r)PitIcoho 025 92+0.1134xrit1c0110 025 C)3)+1 RiPitCh @25 C
1¨ (0.4597 xPPitch @,25 C 0.2425 X (PPit1C 0h07.25 C)2 +0.1134X(PPicc0/10 025 93) =
l000 2 X (0A597 X1210010.0"-0.2425X(1210010.093)2+0.1134x(1210010:3)3)+1 RiPitch @25 C =
1¨ (0.4597 X12 1.93 0.242541"1.93)2+0.1134412 1-93)3) R/PitCh @25 C = 1.7299 Example 3.3.7 Calculate FRI of pitch:

[00164] Solving equation (5) for FRIPitch @25 C:
= (RI pitch @25 02-1 FRI pitch @25 C (Ripitch@2s 02+2 (5b) Where FR/Pitch @25 C: FRI of the Pitch at 25 C; and RiPitch @25 C: Refractive index of the Pitch at 25 C (Ex 3.3.1).

[00165] Solving:
(Ripitch@25.02-1 1.72992 ¨1 FRI pitch @25 C (RI picth 025.Cõ+2 = 1.72992+2 = 0.3991 Example 3.3.8 Calculate the FRI of the PDAO at 25 C:

[00166] Recall equation (6) and solving for FRI of the partially deasphalted oil:
vFeed @25 C XFR/Feed @25 C¨VPitch @25 C)<FRIPitch@25 C
FRI,PDA0 @25 C = (6b) VPDA0 @25 C
Where FRI,PDA0 @25 C: FRI of the partially de-asphalted oil at 25 C, after phase separation has occurred;
vFeed@25 C: Volume % (on Feed basis) of Feed at 25 C (i.e. 100, by definition) FRI Feed @25 C: FRI of the Feed at 25 C (Ex 2.1.3);
V Pitch @25 C: Volume % (on Feed basis) of Pitch at 25 C, after phase separation has occurred (Ex 3.3.3);
FRI pitch @25 C: FRI of the Pitch at 25 C, after phase separation has occurred (Ex 3.3.2);
and VPDA0 @25 C: Volume % (on Feed basis) of partially de-asphalted oil at 25 C, after phase separation has occurred (Ex 3.3.4).

[00167] Solving:
VFeed@25 CXFFIFeed025 C¨VPiteh P25 C XFR1Pitch @25 C
FRI,PDA0 @25 C = = VPDAO @25 C
100x0.3382-8.27x0.3991 FRI,PDA0 @25 C = 91.72 FRI,PDA0 @25 C = 0.3328 Example 3.3.9 Calculate FRI of the S+PDA0 at 25 C:

[00168] Re-arranging equation (6):
FRI,S+PDA0 @25 C '=" (VS+PDA0 @25 C VPDAO @25 C) X FRI,S @25 C VPDAO @25 C X
(28) FRI,PDA0 @25 C
Where:
FRI,S+PDA0 @25 C: FRI value of the solvent-partially de-asphalted oil at 25 C, after phase separation has occurred;
VS+PDAO @25 C: Volume % (on Feed basis) of solvent-partially de-asphalted oil at 25 C, after phase separation has occurred (Ex 3.3.7);
VPDAO @25 C: Volume % (on Feed basis) of solvent at 25 C (Ex 3.3.3);
FRI,S @25 C: FRI value of the solvent at 25 C (within the calculation of Ex 2.2); and FRI,PDA0 @25 C: FRI value of the partially de-asphalted oil at 25 C, after phase separation has occurred (Ex 3.3.8).

[00169] Solving:
FRI of the S+PDA0 at 25 C:
FRI,S+PDA0 @25 C
(VS+PDA0 @25 C VPDAO @25 C) X FRI,S @25 C VPDAO @25 C
X FRI,PDA0 @25 C
FRI S+PDA0 @25 C = (276.31 ¨91.72) x 0.2187 + 91.72 x 0.3328 FRI,S+PDA0 @25 C = 0.2566 Example 3.3.10 Calculate the RI of the S+PDA0 at 25 C:
Equation (11) from Ex 2.1.4 is used to solve the for Ris+pDA0 @250C:
2xFm,s+PDA0 @25 C + 1 R1S+PDA0 @25 C (11b) '¨RI,S+PDA0 @25 C
Where:

RIS+PDA0 @25T: RI of the S+PDA0 at 25 C, after phase separation has occurred;
and FRI,S+PDA0 @25 C: FRI of the S+PDA0 at 25 C, after phase separation has occurred (Ex 3.3.9).

[00170] Solving:
RI of the S+PDA0 at 25 C
2XF RI S+PDA0 @25 C+1 2x0.2566+1 RIS+PDA0 @25 C = = 1.4267 l¨FRJ,s+pDAQ @25 C 1-0.2566 Example 3.3.11 calculate the RI of the S+PDA0 at the extraction temperature:

[00171] Equation (12) from Ex 2.1.5 can be used to calculate RI
S+PDA0 @T C:
2 xms:+pD110 @25oc-1X PS+PDA0 @T C +1 +PDAO @25 C+2 PS+PDA0 @25 C
(10b) RIS+PDA0 @T C =

S+PDA0 @25 C1 xPS+PDA0 @T C
1¨

RI S2 +PDAO @250C+2 PS+PDA0 @25 C
Where:
RIS+PDA0 @TT: RI of the S+PDA0 at the extraction temperature, after phase separation has occurred;
RIS+PDAO @25 C: RI of the S+PDA0 at 25 C, after phase separation has occurred (Ex 3.3.9);
PS+PDA0 @25 C: Density of the S+PDA0 at 25 C, after phase separation has occurred, in kg/m3 (Ex 3.2.9); and PS+PDA0 @T C: Density of the S+PDA0 at the extraction temperature, after phase separation has occurred, in kg/m3 (Ex 3.2.9).

[00172] Solving:
R1+PDA0 @25 C1 PS+PDA0 @165 C+ , 2X 7 X i 2x 1.42672-1x579.03 +1 1.42672+2 751.37 RIS+PDA0 @165 C RI-S+PDA0 @25 C+2 PS+PDA0 @25 C
Ris2+pDA0g25.C- X1 PS+PDA0 @165 C 1-1.42672-1 X
579.03 1.3189 RI-s+pDA0 @250C+2 PS+PDA0 @25 C 1.42672+2 751.37 Example 4 Check whether the two methods of calculating the RI of S+PDA0 at the extraction temperature have converged:

[00173] Recall, the RI of the S+PDA0 calculated in Ex 2 and 3 are:
Rirtae gtheof.1s1+pDA0 165 C = 1.32 1 5 (Ex 2.4) gtheoc11 s2+pDA0 165 C = 1.3189 (Ex 3.3.11)

[00174] Since RIrtaetgheqii-i-PDA0 @165 C # RIrtaegthev+pDA0 @165 C' Ex 3 is iterated using new guesses until the RI values converge.

[00175] If RI
rtae gtheV+PDA0 @165 C < RCae gtheV+PDA0 @165 C, the guessed S/F Ratio in Ex 3 is decreased.

[00176] If RIPtaagheoft 5?+pDA0 _ @165 C > RIrtaetgheoly+pDA0 165 C, the guessed S/F Ratio in Ex 3 is increased.

[00177] The guessed value of the selected operating parameter at the convergence of the RI values calculated using Method 1 and Method 2 is the controlled value of the selected operating parameter.

[00178] The above description is meant to be exemplary only, and one skilled in the relevant arts will recognize that changes may be made to the embodiments described without departing from the scope of the disclosure. For example, the operations represented in the drawing described herein are for purposes of example only. There may be many variations to these operations without departing from the teachings of the present disclosure. For instance, the operations may be performed in a differing order, or operations may be added, deleted, or modified. The present disclosure may be embodied in other specific forms without departing from the subject matter of the claims. Also, one skilled in the relevant arts will appreciate that while the systems, devices and assemblies disclosed and shown herein may comprise a specific number of elements/components, the systems, devices and assemblies could be modified to include additional or fewer of such elements/components. The present disclosure is also intended to cover and embrace all suitable changes in technology.
Modifications which fall within the scope of the present invention will be apparent to those skilled in the art, in light of a review of this disclosure, and such modifications are intended to fall within the scope of the appended claims.

[00179] Every document, including publications and published patent documents, cited herein is hereby incorporated herein by reference in its entirety. The citation of any document is not an admission that it is prior art with respect to the present disclosure.
Further, to the extent that any meaning or definition of a term in this document conflicts with any meaning or definition of the same term in a document incorporated by reference, the meaning or definition assigned to that term in this document shall govern.

Claims (12)

WHAT IS CLAIMED IS:

1. A method for solvent de-asphalting comprising:
selecting a solvent based on RI; and contacting the selected solvent with a feed including asphaltenes to effect de-asphalting.

2. A de-asphalting system for solvent de-asphalting comprising:
a deasphalter, the deasphalter defining:
a contacting zone for contacting a feed, including asphaltenes, and a solvent to form a mixture, wherein the contacting of the feed and the solvent causes at least a portion of the asphaltenes to precipitate out of the mixture, the contacting disposed at an operating temperature; and a separation zone to separate the mixture into a de-asphalted oil-comprising material fraction ("S+PDAO") and a asphaltene-rich material fraction, the asphaltene-rich material fraction including the precipitated asphaltenes; and a controller for controlling at least one operating parameter of the deasphalter based on at least on a refractive index of the S+PDAO phase, the operating parameter selected from: the operating temperature; the composition of the feed; the composition of the solvent; a ratio of the mass of precipitated asphaltenes to the mass of asphaltenes within the feed;
and a ratio of the mass of the solvent to the mass of the feed.

3. The de-asphalting system of claim 2 further comprising at least one flow regulator operatively connected to the controller, such that the controller, via the flow regulator, controls the feed flow rate of the feed, a solvent flow rate of the solvent or both.

4. The de-asphalting system of claim 2 further comprising a temperature regulator operatively connected to the controller, such that the controller, via the temperature regulator, controls the operating temperature of the contacting zone.

5. The de-asphalting system of claim 2 further comprising a refractive index determining device operatively connected to the controller.

6. The de-asphalting system of claim 5, wherein the refractive index determining device includes a densitometer, wherein the densitometer is provided for effecting a determination of the refractive index of the S+PDAO, such that the controlling of the at least one operating parameter of the deasphalter, by the controller, is based on at least the refractive index of the S+PDAO phase that is determined by the densitometer.

7. The de-asphalting system of claim 6, wherein the refractive index determining device includes a refractometer, wherein the refractometer is provided for effecting a determination of the refractive index of the S+PDAO, such that the controlling of the at least one operating parameter of the deasphalter, by the controller, is based on at least the refractive index of the S+PDAO phase that is determined by the refractometer.

8. The de-asphalting system of claim 2 wherein the refractive index of the S+PDAO is calculated as a function of the portion of the precipitated asphaltenes, the refractive index of the feed composition, the refractive index of the solvent, the UOP-K
characterization factor of the solvent, and the operating temperature according to the following formulas:

9. A method for solvent de-asphalting comprising:
providing a feed, including asphaltenes, at a feed flow rate;
providing a solvent at a solvent flow rate;
contacting the solvent and the feed at an operating temperature to effect precipitation of at least a portion of the asphaltenes to obtain a S+PDAO and an asphaltene-rich material fraction, wherein the asphaltene-rich material fraction includes the precipitated asphaltenes; and controlling one operating parameter based on at least a refractive index of the S+PDAO, the operating parameter selected from: the operating temperature; the composition of the feed; the composition of the solvent; a ratio of the precipitated asphaltenes to the mass of asphaltenes within the feed; and a ratio of the feed flow rate to the solvent flow rate.

10. A deasphalted oil obtained by a method comprising the steps of:
providing a feed, including asphaltenes, at a feed flow rate;
providing a solvent at a solvent flow rate;
contacting the solvent and the feed at an operating temperature to effect precipitation of at least a portion of the asphaltenes to obtain a S+PDAO and an asphaltene-rich material fraction, wherein the asphaltene-rich material fraction includes the precipitated asphaltenes; and controlling one operating parameter based on at least a refractive index of the S+PDAO, the operating parameter selected from: the operating temperature; the composition of the feed; the composition of the solvent; a ratio of the precipitated asphaltenes to the mass of asphaltenes within the feed; and a ratio of the feed flow rate to the solvent flow rate.

11. A method for solvent de-asphalting comprising:
defining at least the following operating parameters: a composition of a feed including asphaltenes; a target ratio of a mass of removed asphaltenes to the mass of asphaltenes within the feed; an operating temperature for contacting the feed and a solvent; and a ratio of a feed flow rate of the feed to a solvent flow rate of the solvent;
determining an RI of the solvent based at least on calculating the RI of a S+PDAO formed by contacting the feed with the solvent, selecting a solvent based at least on the determined solvent RI, and contacting the selected solvent with the feed at the operating parameters to effect de-asphalting.

12. A method for starting up a solvent deasphalting process comprising:
pre-determining four operating parameters, the operating parameters are selected from:
an operating temperature; a composition of a feed; a composition of a solvent;
a target ratio of a mass of precipitated asphaltenes to a mass of asphaltenes initially within the feed; and a ratio of a feed flow rate to a solvent flow rate determining the non-predetermined operating parameter based on at least an expected RI of an S+PDAO stream generated by the process; and starting up the process using the pre-determined operating parameters and the determined operating parameter.