Process of hydroconversion-distillation of heavy and/or extra-heavy crude oils

Abstract

A process for hydroconversion-distillation of heavy and/or extra-heavy crude oils, which comprises four stages: 1) desalting and separation of the feedstock; 2) catalytic hydrotreating of light fraction (optional); 3) catalytic hydroconversion of heavy fraction, and 4) distillation of hydrotreated products
to provide products that can be processed in conventional refining schemes designed to operate with light and intermediate crude oils.

Claims

1. A process for the hydroconversion-distillation of heavy and extra heavy crude oils to obtain an upgraded crude oil, which comprises desalting a feedstock comprising heavy and/or extra heavy crude oil at atmospheric pressure and at a temperature of 280 C. to 420 C. to obtain a desalted feedstock, passing said desalted feedstock directly to a distillation zone where said desalted feedstock is subjected to a temperature in the range of from 280 to 420 C. at atmospheric pressure to obtain a light fraction and a heavy fraction, said light fraction containing light gas oil, naphtha and middle distillates having a boiling point of below 360 C., said heavy fraction containing asphaltenes and having a boiling point greater than 360 C.; subjecting said light fraction to catalytic hydrotreatment in the presence of hydrogen to obtain a hydrotreated fraction and to remove sulfur and nitrogen compounds; subjecting said heavy fraction to catalytic hydroconversion in the presence of hydrogen to obtain a hydroconverted fraction having a reduced the viscosity and increased the API gravity; and feeding said hydrotreated fraction and said hydroconverted fraction to an atmospheric distillation apparatus to obtain a distilled light and medium fraction containing naphtha and middle distillates for processing in a process for light and medium crude oils and an atmospheric residue, separating said atmospheric residue and feeding to a vacuum distillation column and recovering a light as oil fraction, a heavy gas oil fraction, and a vacuum residue.

2. The process of claim 1, wherein said feedstock comprises crude oil having 3 to 30 API gravity units.

3. The process of claim 2, wherein said feedstock comprises crude oil having 3 to 10 API gravity units.

4. The process of claim 1, wherein said catalytic hydrotreatment of said light fraction is carried out with catalysts of nickel-molybdenum (NiMo) or cobalt-molybdenum (CoMo), in extruded or spherical shape.

5. The process of claim 1, wherein said catalytic hydrotreatment of said light fraction is carried out at a pressure of 10 to 80 kg/cm.sup.2, hydrogen to hydrocarbon ratio of 350 to 3,000 ft.sup.3/bbl, temperature of 280 to 380 C. and the volumetric feed flow related to catalyst volume (LHSV) of 0.5 to 3 h.sup.1.

6. The process of claim 1, wherein said heavy fraction has an initial boiling point above 360 C. and said catalytic hydroconversion of said heavy fraction is carried out in two or more fixed-bed reactors connected in series.

7. The process of claim 6, wherein said fixed-bed reactor comprise three sequential zones having an increased catalyst concentration than a preceding fixed bed.

8. The process of claim 6, wherein the catalysts of the fixed-bed reactors comprise metals selected from the group consisting of Pt, Pd, Ni, Mo and Co, at concentrations of 2 to 15 weight % of each one in the fresh catalysts.

9. The process of claim 8, wherein said metals are selected from the group consisting of Ni, Mo and Co.

10. The process of claim 8, wherein said catalysts are supported on aluminum oxides, silica, titanium, and mixtures thereof, and where said reactor has a first bed having a catalyst concentration of 0.1-3 wt %, Ni and 1-5 wt % Mo, a second bed having a catalyst concentration greater than said first bed and having catalyst concentration of 0.5-5 wt % Ni and 2-8 wt % Mo, and a third bed having a catalyst concentration greater than said second bed and having a catalyst concentration of 1-5 wt % Ni and 5-12 wt % Mo.

11. The process of claim 10, wherein said support is aluminum oxide in its gamma phase and particle sizes ranging from 1 to 3 mm diameter in cylindrical or extruded with different profiles, tablets or lobular shapes.

12. The process of claim 7, wherein a first zone of said three zones is loaded with a hydrodemetallization catalyst in concentrations of 0.1 to 3 weight % of nickel and from 1 to 5 weight % of molybdenum, supported on gamma alumina.

13. The process of claim 12, wherein an intermediate zone is loaded with a hydrogenation-hydrocracking catalyst in concentrations of 0.5 to 5 weight % of nickel and 2 to 8 weight % of molybdenum, supported on gamma alumina and where said catalyst concentration of said intermediate zone is greater than said first zone.

14. The process of claim 13, wherein a third zone is loaded with a hydrogenating catalyst in concentrations of 1 to 5 weight % of nickel and from 5 to 12 weight % of molybdenum supported on gamma alumina, and where said catalyst concentration of said third zone is greater than said intermediate zone.

15. The process of claim 6, wherein said catalytic hydroconversion of said heavy fraction is carried out at a pressure of 40 to 130 kg/cm.sup.2, a hydrogen to hydrocarbon ratio of from 2,000 to 7,000 feet.sup.3/bbl, a temperature of 320 to 450 C. and the volumetric feed flow related to catalyst volume (LHSV) of 0.2 to 3 h.sup.1.

16. The process of claim 1, wherein said vacuum residue has an API gravity higher than 22 units.

17. The process of claim 1, wherein said process increases the volumetric yield of the fractions obtained from a heavy and/or extra-heavy crude oils: light naphtha up to 1%, intermediate naphtha up to 2%, heavy naphtha up to 3%, light distillate up to 4%, heavy distillate up to 7%, straight-run gas oil up to 5%, light vacuum gas oil up to 12%, and heavy vacuum gas oil up to 5%; in addition to a decrease of the vacuum residue as high as 30%.

18. The process of claim 1, wherein said process removes impurities contained in heavy and/or extra-heavy crude oils: hydrodemetallization up to 90%, hydrodesulfurization up to 90%, hydrodenitrogenation up to 70%, carbon removal up to 60%, and asphaltenes removal up to 70%.

19. A process for the hydroconversion-distillation of extra heavy crude oils to obtain an upgraded crude oil, which comprises desalting a feedstock comprising an extra heavy crude oil at atmospheric pressure and at a temperature of 280 C. to 420 C. using fresh water to obtain a desalted extra heavy crude oil feedstock, passing the desalted extra heavy crude oil feedstock directly to a distillation column to separate the desalted extra heavy crude oil feedstock into a light fraction and a heavy fraction, said light fraction containing light gas oil having a boiling point below 360 C. and said heavy fraction having an initial boiling point above 360 C.; subjecting said light fraction to catalytic hydrotreatment in the presence of hydrogen to reduce the concentration of sulfur and nitrogen compounds and to obtain a hydrotreated light fraction; subjecting said heavy fraction to catalytic hydroconversion in the presence of hydrogen in a fixed-bed reactor having a first bed, a second bed, and a third bed connected in series with hydrogen added to an inlet and along the catalyst beds of the second reactor, each of said fixed-bed reactors contains a NiMo catalyst supported on gamma alumina and where said first bed comprises a catalyst having 0.1-3 wt % No and 1-5 wt % Mo, a second bed comprising a catalyst having 0.5 to 5 wt % Ni and 2-8 wt % Mo and has a catalyst concentration greater than said first bed, and a third bed comprising a catalyst having 1-5 wt % Ni and 5-12 wt % Mo and a catalyst concentration greater than said second bed, said catalytic hydroconversion being carried out to remove sulfur and nitrogen compounds from said heavy fraction and increase the API gravity; and feeding said hydrotreated light fraction and said catalytic hydroconversion heavy fraction to an atmospheric distillation column to obtain a first fraction containing a light and medium crude oil fraction and an atmospheric residue fraction, subjecting said atmospheric residue fraction to vacuum distillation to obtain a vacuum light gas oil, a vacuum heavy gas oil, and a vacuum residue.

20. A process for the hydroconversion-distillation of heavy and extra heavy crude oils, consisting essentially of, in order: a. desalting a feedstock comprising heavy and/or extra heavy crude oil using fresh water at atmospheric pressure and at a temperature of 280 C. to 420 C. to obtain a desalted feedstock, b. passing said desalted feedstock to an atmospheric distillation zone where said desalted feedstock is subjected to a temperature in the range of from 280 to 420 C. at atmospheric pressure to obtain a light fraction having a boiling point below 360 C. and a heavy fraction having a boiling point above 360 C., said light fraction containing light gas oil; and c. subjecting said light fraction to catalytic hydrotreatment in the presence of hydrogen to obtain a hydrotreated light fraction and subjecting said heavy fraction to catalytic hydroconversion in the presence of hydrogen to obtain a hydroconversion heavy fraction; and feeding said hydrotreated light fraction and said hydroconvertion heavy fraction to an atmospheric distillation column to obtain first fraction containing light and medium distilled crude oil fractions for processing in refining schemes designed to process light and medium crude oils and an atmospheric residue, and feeding said atmospheric residue to a vacuum distillation column and recovering a vacuum light gas oil, a vacuum heavy oil and a vacuum residue.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 shows a process flow diagram of the present invention: hydroconversion-distillation of heavy and/or extra-heavy crude oils, more specifically referring to the catalytic hydroconversion of heavy and/or extra-heavy crude oils, and atmospheric and vacuum distillations of the hydrotreated product.

DETAILED DESCRIPTION OF THE INVENTION

(2) The present invention relates to a process of the petroleum refining industry: hydroconversion-distillation of heavy and/or extra-heavy crude oils, more specifically to the catalytic hydroconversion of heavy and/or extra-heavy crude oils, and atmospheric and vacuum distillations of the hydrotreated product.

(3) In this respect, it is important to point out that, by means of the process of the present invention such products that can be processed in conventional refining schemes designed to operate light and intermediates crudes are obtained.

(4) The process of the present invention processes feedstocks with API gravity in the range of 3 to 30 API, and because of the nature of the feeds it comprises preheating of the same feed and feeding lines, in order to comply with optimal properties for transport (particularly viscosity) to the crude oil fractionation zone. Preheating of the feed can be carried out by heat exchange with hot streams of the same unit, while the heating pipes can be carried out using steam jackets. Under these conditions, it is necessary to guide the settlement process and equipment to optimize the energy balance when dealing with streams of high molecular weight and high viscosities.

(5) FIG. 1 shows a process flow diagram of the present invention, which comprises four stages:

(6) 1) Desalting and separation of the feedstock;

(7) 2) Catalytic hydrotreating of the light fraction (optional);

(8) 3) Catalytic hydroconversion of the heavy fraction, and

(9) 4) Distillation of the hydrotreated products.

(10) Step 1) Desalting and separation of the feedstock, that can be considered as a preparation of the feedstock (heavy and/or extra-heavy crude oils) to steps 2) and 3), consisting in desalting the heavy and/or extra-heavy crude oil, and adjusting the boiling range of light and heavy cuts, operating at atmospheric pressure and temperature of 280 to 420 C., prior to stages of hydrotreating and catalytic hydroconversion of said fractions, respectively. Step 2) catalytic hydrotreating of the light fraction is optionally carried out and would be performed at less severe operating conditions than those of step 3) catalytic hydroconversion of heavy fraction.

(11) In this regard it is important to note that the separate treatment of these two fractions brings benefits on reduced investment and operating costs as the two fractions are hydrotreated by using different catalysts, operating conditions and type of reactors. Adjusting the boiling temperature of the two fractions is carried out by distillation. Typically, the light fraction comprises hydrocarbons with a boiling temperature below 360 C., while the heavy fraction comprises compounds with higher boiling temperature than this temperature until the final boiling point of the petroleum feedstock. These values are defined depending on the type and quality of petroleum feedstock and refining scheme.

(12) For example, in an extra-heavy crude oil the light fraction can be very small if the fractionation is carried out at a very low final boiling temperature, so that the fractionation temperature is raised to increase the volume of this fraction. On the other hand, in a heavy crude oil the light fraction can be bigger and would require a decrease in the final temperature cut during fractionation. These decisions are made based on the type of crude to be processed, the operating conditions of the reactors, the size of the reactors (processing capacity) and on the desired properties of the final product.

(13) The process of the present invention has the flexibility to operate under different qualities of the feedstock and required products.

(14) In step 2) catalytic hydrotreating of the light fraction, due to its boiling temperature range (the initial boiling point of petroleum and cutting temperature in the first stage), the light fraction can mainly contain impurities of sulfur and nitrogen. The complexity of the molecules includes up to alkyl benzothiophenes, whose difficulty for removal occurs by steric hindrances. This fraction contains cuts of the type of naphthas, middle distillates and a small fraction of gasoils. The relative composition of each cut depends on the type of petroleum feed and the final boiling temperature of the light fraction.

(15) The catalytic hydrotreatment of this light fraction can be carried out in a conventional reactor operating with catalysts of nickel-molybdenum (NiMo) or cobalt-molybdenum (CoMo), in extruded form. The operating conditions of the reaction zone for the catalytic hydrotreatment are: operating pressure of 10 to 80 kg/cm.sup.2, hydrogen to hydrocarbon ratio of 350 to 3,000 ft.sup.3/bbl, temperature of 280 to 380 C. and liquid hourly space velocity (LHSV) of 0.5 to 3 h.sup.1; all other operating conditions of the catalytic hydrotreatment plant will be those provided in similar conventional units.

(16) A variant of the process of the present invention is that it has the option of whether or not hydrotreat the light fraction mainly depending on the required quantity and quality of the products, because if the crude oil feedstock is so heavy, the volume of this fraction is very small. In this circumstance, it is desirable to directly feed this light fraction to atmospheric distillation column of step 4).

(17) Step 3) catalytic hydroconversion of heavy fraction that has several purposes: on the one hand the reduction of content of impurities such as organometallic, sulfur and nitrogen compounds, and on the other hand reducing viscosity and increasing the API gravity of the feedstock. The catalytic hydroconversion is carried out in two or more fixed-bed reactors connected in series, the catalytic beds are loaded with three types of extrudate catalysts in different proportions. Each catalytic bed preferably has a catalyst concentration that is higher than the preceding catalyst bed such that the catalyst concentration increases from the feed end to the outlet end.

(18) One of the properties of the catalytic bed is to have a hydrogenating function, which is achieved with catalysts containing metals that have the property to chemisorb hydrogen atoms such as: Pt, Pd, Ni, Mo and Co, among others, preferably Ni, Mo and Co, for their resistance to sulfur poisoning, in concentrations from 2 to 15 weight % each in the fresh catalyst.

(19) Another important function of the catalyst bed is to retain the heavy metals containing in the heavy oil, mainly Ni, V, Fe, Cu and Pb; consequently a support is selected with high porosity such as oxides of aluminum, silica, titanium and mixtures thereof, these supports should also have adequate mechanical properties for reactor operation at high pressures and temperatures, and adequate size to avoid high pressure drops. The most suitable catalysts for this process typically use aluminum oxide support (alumina) in its gamma phase and particle sizes ranging from 1 to 3 mm diameter either cylindrical or extruded shapes with different profiles, tablets, or lobular.

(20) An additional function of the catalyst bed used in the process of the present invention is to convert the sulfur and nitrogen compounds in the feedstock to hydrogen sulfide and ammonia, respectively; which is accomplished, to some extent, taking advantage of the catalyst property of chemisorb atoms of hydrogen, sulfur and nitrogen, whose function is properly performed by the active metals Ni and Mo in sulfide form by breaking the CSC and CNC bonds and saturate the sulfur and nitrogen to form hydrogen sulfide and ammonia respectively.

(21) First in the catalyst bed a hydrodemetallization catalyst is loaded whose function is to partially hydrogenate the molecules of the heavy compounds, for which the catalyst has a relatively low hydrogenating function capable to hydrocrack; the catalyst permits reactions to favor removal of heavy metals. Such a catalyst contains low amounts of nickel and molybdenum supported on gamma alumina in concentrations of 0.1 to 3 weight % of nickel and 1 to 5 weight % of molybdenum.

(22) The intermediate portion of the catalyst bed has hydrogenation-hydrocracking balanced functions, hydrogenation function allows more reactions for promoting the removal of sulfur and nitrogen as well as the saturation of aromatics present in the separate chains of large molecules by the effect of the hydrocracking function, to meet these objectives, the catalyst of the intermediate zone of the catalytic bed is formulated with 0.5 to 5 weight % of nickel and from 2 to 8% by weight of molybdenum. The catalyst concentration in the intermediate zone is preferably higher than in the first catalyst bed.

(23) The final part of the catalyst bed is loaded with a catalyst, mainly for the hydrogenating function to favor the removal of sulfur and saturation of the hydrogen deficient species; the concentrations of active metal in this catalyst are 1 to 5% by weight of nickel and 5 to 12 weight % of molybdenum. The catalyst concentration in the final bed is preferably higher than in the intermediate zone.

(24) The three types of catalysts are loaded into the reactor using the procedures applicable to the industrial scale, in addition to the catalyst bed relaxer pressure drop materials that may or may not have catalytic activity for hydrogenation, hydrocracking, or both must be loaded. Different profiles of shape can be used in the active catalysts such as cylindrical extruded, lobe or spheres in sizes ranging from 1 to 3 millimeters in diameter. Relaxants materials may also have different shape, including: spheres, tablets, raschig rings and similar.

(25) In order to adequately fulfill the processing of crude oil, the process of the present invention employs at least two fixed-bed reactors, with the arrangement of several reactors having the following main advantages: adequately exploit the function of each catalyst throughout the reactor; reduce the problems of pressure drop across the catalyst beds, and add additional amounts of hydrogen between the different reactors and thereby maintain a proper hydrogen/hydrocarbon ratio (H.sub.2/HC) in each reactor, thus decreasing the effects of high temperature in the catalytic bed derived from the evolution of heat.

(26) As a result of the exothermic nature of the reactions, it is necessary to add hydrogen streams along the catalyst bed and the inlet of the second reactor, the effect of addition of the hydrogen stream is: replacing the hydrogen consumed in the first reactor in order to maintain a suitable ratio of hydrogen/hydrocarbon in the second reactor; controlling the generation of heat and control the system temperature in the needed values to ensure the proper operation of the reactors, and limit the formation of carbon reactions and its deposit on the surface of the catalyst.

(27) The operating conditions of the reaction zone are: pressure of 40 to 130 kg/cm.sup.2, temperature of 320 to 450 C., hydrogen/hydrocarbon ratio from 2,000 to 7,000 ft.sup.3/bbl, and space velocity (LHSV) of 0.2 to 3 h.sup.1. Depending on the quality of the feedstock and the desired results in products of the process, it is possible to combine these different values of operating variables.

(28) Step 4) Distillation of the hydrotreated products, that comprises the feeding of the light and heavy fractions obtained in steps 2) and 3) to an atmospheric distillation column.

(29) The light fraction fed to the atmospheric column might be hydrotreated or not, depending on their levels of contaminants such as sulfur or nitrogen and especially its volumetric content in the petroleum feed; the point of feeding of the light fraction obtained in step 2) to the atmospheric distillation column depends on the particular design of this column and is usually fed into the intermediate portion of the column, depending on its composition and temperature profile of the column.

(30) Moreover, the heavy fraction obtained in step 3) is always added to the bottom of the atmospheric distillation column.

(31) In this primary distillation naphtha and middle distillates cuts are obtained, and the atmospheric residue as well; the latter is fed to the vacuum distillation column where the light and heavy vacuum gasoils cuts and vacuum residue are obtained. All fractionated cuts in both the primary and vacuum distillation columns, are sent to the various downstream refining processes.

(32) Among the main technical contributions of the process of the present invention, compared with conventional refining processes are the following: increases the yield of distillate fractions and decreases the concentration of pollutants such as: sulfur, nitrogen, metals, etc., favoring the downstream plants operating at less severe conditions with the consequent increase in the lifetime of the catalysts and the reduced operating costs by reducing the consumption of utilities. allows existing and conventional refineries to process larger amounts of heavy and extra-heavy crude oils. Existing and conventional refineries means those that were designed for processing light and intermediates crude oils and their mixtures, in particular those having API gravity higher than 22 units. The light and heavy fractions obtained can be fed to the atmospheric distillation column in existing refineries, because their properties are similar to those of light and intermediates crude oils which are usually processed. For example, it is possible to increase the API gravity of the heavy fraction due to the addition of hydrogen to the poly aromatic molecules of the crude and thus not disturbing the operation of the atmospheric column. It also increases the yield of distillates of high commercial value.

EXAMPLES

(33) To better illustrate the process of the present invention, below are some examples, which do not limit the scope of what is claimed herein.

Example 1

(34) A heavy crude oil with 15.93 API and complimentary properties presented in Table 1, was subjected to step 1) Desalting and separation of the feedstock, of the process of the present invention, obtaining a light fraction and a heavy fraction with 42.61 and 6.78 API, respectively, among other properties shown in Table 1.

(35) TABLE-US-00001 TABLE 1 Properties of heavy crude oil under step 1) Desalting and separation of the feedstock, of the process of the present invention, and light and heavy obtained fractions, (Example 1). Heavy Fraction Properties Crude oil Light Heavy Yield, volume %. 100 29.1 70.9 API Gravity 15.93 42.61 6.78 Sulfur, weight % 4.602 1.748 5.52 Conradson carbon, weight % 15.87 19.80 n-heptane-lnsolubles, weight % 15.66 20.57 Nickel, wppm 69.20 104 Vanadium, wppm 361.0 501 Distillation, volume %. D-2892 D-86 D-1160 IBP/10 28/173 60/117 369/397 20/30 266/353 145/171 440/491 40/50 432/504 197/226 60/70 247/270 80/90 286/305 FBP 538 321 538 Recovered at 538 C., volume %. 54.59 38.01 IBP: Initial Boiling Point TFE: Final Boiling Point

(36) From Table 1, it is important to emphasize the zero contents of n-heptane-insolubles (asphaltenes), nickel and vanadium in the light fraction, which ensures that the catalysts used in step 1) desalting and separation of the feedstock, do not experience significant deactivation during the time-on-stream. Such impurities are concentrated in the heavy fraction which is fed to step 2) catalytic hydrotreating of the light fraction, wherein the catalysts used here suitable properties for accumulating heavy metals, and breaking the complex molecules of asphaltenes to produce lighter distillates.

(37) The light fraction obtained in the step 1 of Example 1 was subjected to a second step 2) Catalytic hydrotreating of the light fraction, of the process of the present invention, at the operating conditions indicated in Table 2.

(38) TABLE-US-00002 TABLE 2 Operating conditions of step 2) Catalytic hydrotreating of the light fraction, of the present invention, obtained in step 1), (Example 1). Variable Condition Pressure, kg/cm.sup.2 54 Temperature, C. 340 Space velocity (LHSV), h.sup.1 2.5 H.sub.2/HC ratio, feet.sup.3/bbl 2,000

(39) The properties of the product obtained in step 2) of Example 1, are shown in Table 3.

(40) TABLE-US-00003 TABLE 3 Properties of the hydrotreated light fraction, obtained in step 2) Catalytic hydrotreating of the light fraction, of the process of the present invention, (Example 1). Property Value Yield, volume %. 100.32 Specific gravity 60/60 F. 0.8030 API Gravity 44.71 Sulfur, weight % 0.048 Distillation, volume %. IBP/10 76/127 20/30 151/172 40/50 197/220 60/70 240/259 80/80 279/300 FBP 321 IBP: Initial boiling point FBP: Final Boiling Point

(41) From Table 3 it is important to note the considerable reduction of sulfur content in the product, from 1,748 weight % of sulfur in the light fraction (Table 1) to 0.048 weight % of sulfur in the product (Table 3).

(42) The heavy fraction obtained in step 1) of Example 3 was subjected to Step 3) catalytic hydroconversion of heavy fraction, using two fixed-bed reactors connected in series at the operating conditions shown in Table 4.

(43) TABLE-US-00004 TABLE 4 Operating conditions of step 3) Catalytic hydroconversion of the heavy fraction, of the present invention, obtained in step 1), (Example 1). Variable Reactor 1 Reactor 2 Pressure, kg/cm.sup.2 100 100 Temperature, C. 386 386 Space velocity (LHSV), h.sup.1 0.25 0.25 H.sub.2/HC ratio, feet.sup.3/bbl 5,000 5,000

(44) Product properties obtained in the step 3) of Example 1, are shown in Table 5.

(45) TABLE-US-00005 TABLE 5 Properties of the hydroconverted heavy fraction, obtained in step 3) catalytic hydroconversion of the heavy fraction, of the process of the present invention, (Example 1). Hydroconverted Property heavy fraction Yield, volume % 104.57 API Gravity 18.17 Sulfur, weight % 0.8583 Conradson carbon, weight % 9.76 n-heptane-Insolubles, weight % 8.64 Nickel, ppm 42.40 Vanadium, ppm 132.50 Distillation, volume % IBP/10 225/328 20/30 375/407 40/50 446/491 60/70 530/ 80/90 FBP 538 Recovered at 538 C., volume % 62.85 IBP: Initial boiling point FBP: Final Boiling Point

(46) From Table 5, it is important to underline the considerable increase in API gravity: from 6.78 in the heavy fraction (Table 1) to 18.17 in the product (Table 5), ensuring higher production of valuable distillates.

(47) The hydrotreated light and hydroconverted heavy fractions obtained in stages 2) and 3) of Example 1 were subjected to step 4) Distillation of the hydrotreated products, of the present invention. The yields and properties of the distillates obtained from this fractionation are shown in Table 6.

(48) TABLE-US-00006 TABLE 6 Properties and yields of the distillates obtained in step 4) Distillation of the hydrotreated products, of the process of the present invention, (Example 1). Distillation Yield, Sulfur, range, volume Specific Gravity weight Fraction C. % gravity API % Light naphtha IBP-71 1.58 0.6608 82.63 0.0033 Medium naphtha 71-177 10.02 0.7492 57.37 0.0077 Heavy naphtha 177-204 4.56 0.7953 46.42 0.0084 Light distillate 204-274 11.66 0.8281 39.37 0.0093 Heavy distillate 274-316 8.78 0.8559 33.82 0.0169 Light gasoil 316-343 5.40 0.8734 30.51 0.1172 Light vacuum 343-454 22.16 0.9012 25.51 0.2120 gasoil Heavy vacuum 454-538 11.34 0.9247 21.52 0.2807 gasoil Vacuum residue 538 C.+ 24.5 1.0264 6.36 1.8973 IBP: Initial boiling point

(49) From Table 6 it is important to note the significant reduction in the recovered fraction at 538 C., volume % or vacuum residue, from 54.59 volume % in the heavy oil feed (Table 1) to 24.5 volume % in the product (Table 6). This reduction increases the production of other distillates.

Example 2

(50) A heavy crude oil with 21.24 API and other properties presented in Table 7, was subjected to step 1) desalting and separation of the feedstock of the present invention, obtaining light and heavy fractions with 42.98 and 6.97 API respectively, among other properties presented in Table 7.

(51) TABLE-US-00007 TABLE 7 Properties of heavy oil, under the step 1) Desalting and separation of the feedstock, of the process of the present invention, and light and heavy obtained fractions, (Example 1). Fraction Property Crude Light Heavy Yield, volume %. 100 43.86 56.14 API gravity 21.24 42.98 6.97 Sulfur, weight % 3.501 1.1921 4.78 Conradson carbon, weight % 10.48 17.61 n-heptane-Insolubles, weight % 9.51 17.72 Nickel, ppm 52.64 87.6 Vanadium, ppm 247.7 411.5 Distillation, volume %. D-2892 D-86 D-1160 IBP/10 13/130 48/125 366/447 20/30 199/269 150/175 487/533 40/50 344/423 200/225 60/70 509/ 250/276 80/90 300/331 FBP 538 373 538 Recovered at 538 C., volume %. 63.2 31.3 IBP: Initial boiling point FBP: Final Boiling Point

(52) The light fraction obtained in the step 1) of Example 2, was subjected to a second step 2) Catalytic hydrotreating of the light fraction, of the process of the present invention, at operating conditions indicated in Table 8.

(53) TABLE-US-00008 TABLE 8 Operating conditions of step 2) catalytic hydrotreating of the light fraction, of the process of the present invention, obtained in step 1), (Example 2). Variable Condition Pressure, kg/cm.sup.2 54 Temperature, C. 340 Space velocity (LHSV), h.sup.1 2.5 H.sub.2/HC ratio, feet.sup.3/bbl 2,000

(54) Product properties obtained in step 2) of Example 2 are shown in Table 9.

(55) TABLE-US-00009 TABLE 9 Properties of the hydroconverted light fraction, obtained in step 2) catalytic hydrotreatment of the heavy fraction, of the process of the present invention, (Example 2). Property Value Yield, volume %. 100.26 Specific gravity 60/60 F. 0.8053 API gravity 44.21 Total sulfur, weight % 0.044 Distillation, volume %. IBP/10 46/123 20/30 148/173 40/50 198/223 60/70 248/274 80/90 298/329 FBP 372 IBP: Initial boiling point FBP: Final Boiling Point

(56) The heavy fraction obtained in step 1) of Example 2 was subjected to Step 3) Catalytic hydroconversion of the heavy fraction, of the process of the present invention, using two fixed-bed reactors connected in series at the operating conditions shown in Table 10.

(57) TABLE-US-00010 TABLE 10 Operating conditions of step 3) catalytic hydroconversion of the heavy fraction, of the process of present invention, obtained in step 1), (Example 2). Variable Reactor 1 Reactor 2 Pressure, kg/cm.sup.2 100 100 Temperature, C. 400 400 Space velocity (LHSV), h.sup.1 1.0 0.5 H.sub.2/HC ratio, feet.sup.3/bbl 5,000 5,000

(58) Properties of the product obtained in step 3) of Example 2 are shown in Table 11.

(59) TABLE-US-00011 TABLE 11 Properties of the hydroconverted heavy fraction, obtained in step 3) catalytic hydroconversion of the heavy fraction, in the process of the present invention (Example 2). Hydroconverted Property heavy fraction Yield, volume %. 103.3 API gravity 19.06 Sulfur, weight % 0.982 Conradson carbon, weight % 8.63 n-heptane-Insolubles, weight % 8.59 Nickel, ppm 45 Vanadium, ppm 156.5 Distillation, volume %. IBP/10 62/264 20/30 340/378 40/50 403/439 60/70 488/530 80/90 FBP 538 Recovered at 538 C., volume %. 72.6 IBP: Initial boiling point FBP: Final Boiling Point

(60) The hydrotreated light and hydroconverted heavy fractions obtained in stages 2) and 3) of Example 2, were subjected to step 4) distillation of the hydrotreated products, of the present invention. The yields and properties of the distillates obtained from this fractionation are shown in Table 12.

(61) TABLE-US-00012 TABLE 12 Properties and yields of the distillates obtained in step 4) distillation of the hydrotreated products, of the process of the present invention, (Example 2). Distillation Yield, Total range, volume Specific API sulfur, Fraction C. % gravity Gravity weight % Light naphtha IBP-71 2.4 0.6849 75.10 0.0027 Medium naphtha 71-177 14.6 0.7644 53.61 0.0058 Heavy naphtha 177-204 4.5 0.8038 44.54 0.0086 Light distillate 204-274 14.9 0.8340 38.16 0.0099 Heavy distillate 274-316 8.0 0.8644 32.20 0.0164 Light gasoil 316-343 5.3 0.8824 28.86 0.1243 Light vacuum 343-454 23.8 0.9083 24.29 0.2332 gasoil Heavy vacuum 454-538 11.3 0.9438 18.43 0.2744 gasoil Vacuum residue 538 C.+ 15.20 1.0229 6.84 1.8795 IBP: Initial boiling point

Example 3

(62) A heavy crude with 15.93 API and the properties presented in Table 13, was subjected to step 1) desalting and separation of the feedstock, of the process of the present invention, obtaining a light and heavy fractions were with 42.61 and 6.78 API, respectively, among other properties presented in Table 13.

(63) TABLE-US-00013 TABLE 13 Properties of heavy crude oil under step 1) Desalting and separation of the feedstock, of the process of the present invention, and light and heavy obtained fractions, (Example 3). Fraction Property Crude Light Heavy Yield, volume %. 100 29.1 70.9 API gravity 15.93 42.61 6.78 Sulfur, weight % 4.602 1.748 5.52 Conradson carbon, weight % 15.87 19.08 n-heptane-Insolubles, weight % 15.66 20.57 Nickel, ppm 69.2 104 Vanadium, ppm 361.0 501 Distillation, volume %. D-2892 D-86 D-1160 IBP/10 28/173 60/117 369/397 20/30 266/353 145/171 440/491 40/50 432/504 197/226 60/70 247/270 80/90 286/305 FBP 538 321 538 Recovered at 538 C., volume %. 54.59 38.01 IBP: Initial boiling point FBP: Final Boiling Point

(64) The light fraction obtained in the step 1) of Example 3 was not subjected to a second step 2) catalytic hydrotreating of the light fraction, of the process of the present invention.

(65) The heavy fraction obtained in step 1) of Example 3 was subjected to Step 3) catalytic hydroconversion of heavy fraction, of the process of the present invention, using two fixed bed reactors connected in series at the operating conditions shown in Table 14.

(66) TABLE-US-00014 TABLE 14 Operating conditions of step 3) catalytic hydroconversion of the heavy fraction of the process of the present invention obtained in step 1), (Example 3). Variable Reactor 1 Reactor 2 Pressure, kg/cm.sup.2 100 100 Temperature, C. 386 386 Space velocity (LHSV), h.sup.1 0.25 0.25 H.sub.2/HC ratio, feet.sup.3/bbl 5,000 5,000

(67) The properties of the product obtained in step 3) of Example 3 are shown in Table 15.

(68) TABLE-US-00015 TABLE 15 Properties of the hydroconverted heavy fraction, obtained in step 3) catalytic hydroconversion of heavy fraction, of the process of the present invention (Example 3). Hydroconverted Property heavy fraction Yield, volume %. 104.57 API gravity 18.17 Sulfur, weight % 0.8583 Conradson carbon, weight % 9.76 n-heptane-Insolubles, weight % 8.64 Nickel, ppm 42.40 Vanadium, ppm 132.50 Distillation, volume %. IBP/10 225/328 20/30 375/407 40/50 446/491 60/70 530/ 80/90 FBP 538 Recovered at 538 C., volume %. 62.85 IBP: Initial boiling point FBP: Final Boiling Point

(69) The light fraction obtained from step 1) and the hydroconverted heavy fraction obtained in step 3) of Example 3 were subjected to step 4) distillation of the hydrotreated products, of the present invention. The yields and properties of the distillates obtained from this fractionation are shown in Table 12.

(70) TABLE-US-00016 TABLE 16 Properties and yields of the distillates obtained in step 4) distillation of the hydrotreated products, of the process of the present invention, (Example 2). Distillation Yield, Sulfur range, volume Specific Gravity total, Fraction C. % gravity API weight % Light naphtha IBP-71 1.7 0.6657 81.06 0.0290 Medium naphtha 71-177 10.75 0.7528 56.46 0.2338 Heavy naphtha 177-204 3.11 0.7990 45.6 0.6729 Light distillate 204-274 13.04 0.8330 38.37 0.8978 Heavy distillate 274-316 11.40 0.8666 31.78 0.9635 Light gasoil 316-343 7.35 0.8798 29.33 1.0316 Light vacuum 343-454 19.45 0.8933 26.9 0.5509 gasoil Heavy vacuum 454-538 7.38 0.9296 20.72 0.5619 gasoil Vacuum residue 538 C.+ 25.82 1.0253 6.51 2.0212 IBP: Initial boiling point