Process for partial upgrading of heavy and/or extra-heavy crude oils for transportation

Abstract

The present invention relates to a process for the partial upgrading of properties of heavy and/or extra-heavy crude oil by low severity catalytic hydrotreatment in only one reaction step. The process of the present invention is obtained upgraded oil with properties required for its transportation from offshore platforms either to maritime terminal or to refining centers. The process reduces the viscosity of heavy and/or extra-heavy crude oil, and decreases the concentration of impurities, such as sulfur, nitrogen, and metals, in such a way that heavy and/or extra-heavy crude oils can be transported to maritime terminals or to refining centers. The process increases the lifetime of the catalyst and decreased operating costs by reducing consumption of utilities because the operation of the process is carried out at lower severity. The partially upgraded oils obtained in this process can be transported directly to the maritime terminals or to existing refineries.

Claims

1. A process for partial upgrading of properties of heavy and/or extra-heavy crude oils, by catalytic hydrotreatment, which comprises the following steps: 1) desalting of the heavy or extra-heavy crude oil; 2) catalytic hydrotreating of the heavy and/or extra-heavy desalted crude oil at maximum temperatures of 400 C. and 100 kg/cm.sup.2 of pressure or less in a single reaction step to obtain a partially upgraded crude oil, wherein the catalytic hydrotreating step includes a catalyst having a metal loading of molybdenum from 2 to 8 weight % and nickel or cobalt from 0.1 to 3 weight % in the catalyst, supported on gamma alumina, with a surface area of 180 to 200 m.sup.2/g, pore volume of 0.7 to 0.8 cm.sup.3/g, and having a shape profile selected from the group consisting of cylindrical extrudates, lobular and spheres with a diameter of 1 to 3 mm; and 3) separation of partially upgraded oil; wherein said heavy and/or extra heavy crude oils have an API gravity of 3-16 units, and said partially upgraded oil has a kinematic viscosity equal to or less than 250 cSt at 37.8 C., and API gravity increase of 4 to 8 degrees and where said upgraded oil has better quality for its transportation from platforms to maritime terminals or to refining centers.

2. The process according to claim 1, wherein the desalters employed in step 1) are of the dielectric type, for crude oil containing less than 200 pounds salt per 1,000 barrels.

3. The process according to claim 1, wherein step 1) is carried out under pressure of 7 to 14 kg/cm.sup.2 and temperature of 125 to 150 C.

4. The process according to claim 1, wherein in step 1) the pressure value is preferably at least 2 kg/cm.sup.2 above the vapor pressure of a crude oil-water mixture at the operating temperature.

5. The process according to claim 1, wherein the catalytic hydrotreatment of crude oil in step 2) is performed in a fixed bed reactor with a catalyst containing metals selected from the group consisting of Pt, Pd, Ni, Mo and Co.

6. The process of claim 1, wherein the catalytic hydrotreatment is carried out in a fixed bed reactor with a catalyst selected from the group consisting of Ni, Mo and Co, nickel-molybdenum (NiMo) mixtures and cobalt-molybdenum (CoMo) mixtures supported on a support selected from aluminum oxide (alumina), silicon, titanium and mixtures thereof, wherein said aluminum oxide is in the gamma alumina phase.

7. The process according to claim 1, wherein the catalytic hydrotreatment of crude oil in step 2) in addition to the catalyst bed materials further includes pressure drop relaxers, with or without catalytic activity of hydrogenation, hydrocracking, or both, with shapes selected from the group consisting of spheres, tablets, and raschig rings.

8. The process according to claim 1, wherein step 2) is carried out at pressure of 40 to 100 kg/cm.sup.2, hydrogen-to-hydrocarbon ratio of 2,000 to 5,000 ft.sup.3/bbl, temperature of 360 to 400 C. and space velocity or volumetric flow relative to the volume of catalyst (LHSV: liquid hourly space velocity) of 0.25 to 3 h.sup.1.

9. The process according to claim 1, wherein the separation of the partially upgraded oil in step 3) comprises the step of removing sour gases produced in the hydrotreatment from the partially upgraded oil.

10. The process according to claim 9, wherein up to 63% of sulfur is removed from the partially upgraded oil.

11. The process according to claim 1, wherein up to 66% of the metal (Ni+V) is removed with a global deposit rate equal to 0.0168 weight % per hour, equivalent to a catalyst life of 10 months.

12. The process according to claim 1, wherein the partially upgraded oil has a sediment content is less than 0.04 weight %.

13. A method of transporting heavy and/or extra heavy crude oil including the steps of hydrotreating heavy and/or extra heavy crude oil at a temperature of not higher than 400 C. and pressure of 100 kg/cm.sup.2 or less in a single reaction step to increase the API about 4 to 8 degrees, recovering the partially upgraded crude oil, wherein said recovering step comprises feeding said partially upgraded crude oil from the hydrotreating step to a separator to obtain a gas stream and a liquid stream, separating a hydrocarbon liquid condensate from said gas stream, and combining said hydrocarbon liquid condensate with said liquid stream to obtain said partially upgraded crude oil, and transporting the crude oil through a pipeline.

14. The method of claim 13, wherein said desalting step is carried out under a pressure of 7 to 14 kg/cm.sup.2 and a temperature of 125 C. to 150 C.

15. The method of claim 1, wherein said separation step comprises feeding said partially upgraded crude oil from the hydrotreating step to a separator to obtain a gas stream and a liquid stream, separating a hydrocarbon liquid condensate from said gas stream, and combining said hydrocarbon liquid condensate with said liquid stream to obtain said partially upgraded crude oil.

16. A process for partially upgrading a heavy and/or extra-heavy crude oil comprising the steps of: 1) desalting a heavy or extra-heavy crude oil feed by passing the crude oil feed through two desalters connected in series to obtain a desalted crude oil; 2) catalytic hydrotreating the desalted heavy and/or extra-heavy crude oil in the presence of a catalyst at a maximum temperature of 400 C. and a pressure of 100 kg/cm.sup.2 or less in a single reaction step to obtain the partially upgraded crude oil, wherein said catalyst has a molybdenum content of 2 to 8 weight % and nickel or cobalt content of 0.1 to 3 weight % in the catalyst, supported on gamma alumina, with a surface area of 180 to 200 m.sup.2/g, a pore volume of 0.7 to 0.8 cm.sup.3/g, and having a shape profile selected from the group consisting of cylindrical extrudates, lobular and spheres with a diameter of 1 to 3 mm; and 3) separating said partially upgraded crude oil from the resulting reaction mixture of the hydrotreating step; wherein said heavy and/or extra heavy crude oil has an API gravity of 3-16 units, and said partially upgraded crude oil has a kinematic viscosity equal to or less than 250 cSt at 37.8 C., and API gravity increase of 4 to 8 degrees with respect to said heavy and/or extra heavy crude oil feed.

17. The method of claim 16, wherein said separating step comprises feeding said partially upgraded crude oil from the hydrotreating step to a separator to obtain a gas stream and a liquid stream, separating a hydrocarbon liquid condensate from said gas stream, and combining said hydrocarbon liquid condensate with said liquid stream to obtain said partially upgraded crude oil.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 shows a process flow diagram of the present invention, related to partial upgrading of the properties of heavy and/or extra-heavy crude oils, mainly for transportation; by the catalytic hydrotreatment in one reaction step and operating conditions of low severity.

DETAILED DESCRIPTION OF THE INVENTION

(2) The present invention relates to a process for the partial upgrading of heavy and/or extra-heavy crude oil properties, mainly for its transportation, by catalytic hydrotreatment in one reaction step at operating conditions of low severity. The upgrading of the crude oil reduces the level of impurities, such as sulfur, nitrogen and metal compounds. The partial upgrading treats the heavy and extra heavy crude oil to obtain a crude oil with reduced viscosity to be more amenable to transporting through pipelines and processing facilities.

(3) For purposes of the present invention, the term operating conditions of low severity will be used when referring to processes for crude oil hydrotreating operating at maximum temperatures of 400 C. and pressures of 100 kg/cm.sup.2 or less.

(4) In this regard, it is important to note that by the process of the present invention produces upgraded oils with properties required for transportation from the platforms either to the maritime terminals or to refining centers. The upgraded crude oil preferably has a kinematic viscosity of 230 cSt or less at 37.8 C. and an increased API of 4 to 8 degrees.

(5) The process of the present invention hydrotreats heavy and/or extra-heavy crude oils with API gravity ranging from 3 to 16 units in one reaction step at operating conditions of low severity, mainly for partial upgrading of the properties for their transportation. The upgrading of the crude oil increases the API about 4 to 6 degrees and decreases the viscosity to improve handling and transporting of the crude oil.

(6) FIG. 1 shows a flowchart of the process of the present invention, which comprises three stages:

(7) 1) Desalting of heavy or extra-heavy crude oil;

(8) 2) Catalytic hydrotreating of heavy and/or extra-heavy desalted crude oil

(9) 3) Separation of partially upgraded oil.

(10) Step 1) Desalting of heavy and/or extra-heavy crude oil, preferably comprises an array of two desalination plants, preferably the dielectric type, connected in series for crude oil containing below 200 PTB (Pounds Thousand Barrels, i.e. pounds per 1,000 barrels) of salt to meet the specification of the crude oil fed to the reactor. The salt removal is carried out under pressure of 7 to 14 kg/cm.sup.2 and temperature from 125 to 150 C., where the pressure is preferably at least 2 kg/cm.sup.2 above the vapor pressure of the oil-water mixture operating temperature.

(11) Step 2) Catalytic hydrotreating of heavy and/or extra-heavy uses the desalted crude oil from step 1), which is neither further separated nor further conditioned in any way, as performed in current refineries, according to the prior art reported in the background of the invention. Step 2) is conducted under operating conditions of low severity and is performed in a conventional size plant or a plant built with compact equipment without affecting the properties of partial upgraded oil required for its transportation.

(12) The catalytic hydrotreatment of heavy and/or extra heavy desalted crude oil is performed at low severity operation conditions in one reaction step, preferably using a fixed-bed reactor with a catalyst containing metals, such as Pt, Pd, Ni, Mo and Co, preferably Ni, Mo and Co, more preferably nickel-molybdenum (NiMo) mixtures or cobalt-molybdenum (CoMo) mixtures supported on aluminum oxide (alumina), silicon, titanium and mixtures thereof. In one embodiment, the catalyst support is preferably aluminum oxide in the gamma alumina phase.

(13) One of the properties of the catalyst of the present invention is the hydrogenating function; i.e. the catalyst partially hydrogenates the molecules of heavier compounds, and a hydrocracking capacity, allowing selectively breaking reactions of heavy hydrocarbons. This is achieved with catalysts containing metals such as Pt, Pd, Ni, Mo and Co, etc., preferably Ni, Mo and Co, for its resistance to sulfur poisoning that have the property of chemisorbing hydrogen atoms.

(14) Another important function of the catalyst bed is to retain heavy metals contained in heavy and/or extra-heavy crude oil, mainly, Ni, V, Fe, Cu and Pb. Thus a carrier with high porosity is selected such as aluminum oxides (alumina), silicon, titanium and mixtures thereof, these supports should also have adequate mechanical properties for operation in reactors at elevated pressures and temperatures, and textural properties to guarantee a suitable lifetime. In one embodiment, the catalyst carrier has a surface area of 180 to 200 m.sup.2/g, pore volume of 0.7 to 0.8 cm.sup.3/g and a particle size to avoid high pressure drops. The most appropriate catalysts for the process of the present invention use aluminum oxide in its gamma-alumina phase as a catalyst support. Different profiles of shape can be used to produce the active catalysts such as cylindrical extrudates, lobular or spheres ranging from 1 to 3 millimeters in diameter.

(15) An additional function of the catalyst utilized in the process of the present invention is to convert in a controlled manner the sulfur and nitrogen compounds of the feed to hydrogen sulfide and ammonia, respectively. By selecting the combination of the type of reactor, type of catalyst and operating conditions of low severity, the reaction is oriented towards the hydrocracking of large molecules and the selectivity to the removal or reduction of impurities, allowing the process of the present invention to the exclusion of additional steps for the purification of sour gas produced and sulfur recovery.

(16) The catalyst employed in the present invention preferably has low metal loading. In one embodiment the catalyst has a content of molybdenum from 2 to 8 weight %, and nickel or cobalt from 0.1 to 3 weight % in the fresh catalyst, supported on gamma alumina, with textural properties to ensure adequate life. The catalyst and catalyst support has a surface area of 180-200 m.sup.2/g and pore volume of 0.7 to 0.8 cm.sup.3/g. Different profiles of shape can be used to produce the active catalysts such as cylindrical extrudates, lobular or spheres from 1 to 3 millimeters in diameter.

(17) The catalyst is loaded into the reactor using the procedures industrially applicable, in addition to the catalytic bed relaxers of pressure drop must be loaded, which may or may not have catalytic activity in hydrogenation, hydrocracking or both. Relaxer materials may also have different shapes, such as spheres, tablets, raschig and similar rings.

(18) The operating conditions of the reaction zone for the catalytic hydrotreatment are: maximum pressure of 100 kg/cm.sup.2, hydrogen to hydrocarbon ratio of 2,000 to 5,000 ft.sup.3/bbl, temperature of 360 to 400 C. and space velocity or volumetric flow relative to volume of catalyst (LHSV: liquid hourly space velocity) of 0.25 to 3 h.sup.1. The rest of the operating conditions of the other equipment of the catalytic hydrotreating plant are similar to conventional units. Depending on the quality of the feedstock, it is possible to combine the different values of operating variables to obtain a partially upgraded oil with properties suitable for its transportation.

(19) In summary, step 2) catalytic hydrotreatment of heavy and/or extra-heavy desalted crude oil, is designed to meet several objectives, namely: Reduce the kinematic viscosity of the feedstock to values below 250 cSt measured at 37.8 C., Increase API gravity at value greater than 16 units, and Reduce the content of impurities, mainly organometallic compounds of sulfur and nitrogen. In one embodiment, up to 66% of the metal (Ni+V) is removed with a global deposit rate equal to 0.0168 weight % per hour equivalent to a catalyst life of 10 months. In another embodiment, up to 63% of sulfur is removed from the partially upgraded oil.

(20) Step 3) Separation of partially upgraded oil, which is essential to remove the sour gases produced in the hydrotreated oil, comprises a high pressure and high temperature separator where the reaction product, which is a liquid vapor mixture, is fed directly to obtain gas through the top and liquid through the bottom. These two streams have high energy potential which is used to heat cold process streams through an energy integration. The gas stream exchanges heat with the flow of crude oil being fed to the reactor and the flow of desalinated water, reaching a temperature above 200 C. Wash water is added to solubilize the ammonium salts formed by nitrogen removal from crude oil, the mixture finally reaches the high pressure and low temperature separator tank where three streams are obtained: a gas stream corresponding to hydrogen of recirculation, the hydrocarbon liquid condensate phase, and sour water. A fraction of gas stream (3 to 8 volume %) is purged to avoid concentration of light hydrocarbons and hydrogen sulfide in the reaction circuit. This purge is a hydrogen-rich sour stream, the remaining fraction is sent to hydrogen compressor where the recirculation pressure for recycling to the reactor increases. Finally this stream together with make-up hydrogen stream is heated to complete the hydrogen circuit. The liquid stream, product of reactor exchanges heat with the feedstock and the hydrogen streams and is joined with the product hydrocarbon stream of the high pressure and low temperature separator, finally both hydrocarbons streams go to low pressure and low temperature separator where a sour gas stream and the partially upgraded oil are obtained.

(21) Among the main technical contributions of the process of the present invention, compared with conventional processes are the following: It increases the API gravity, decreases the viscosity of heavy and/or extra-heavy crude oil, and reduces in a controlled manner the concentration of impurities such as sulfur, nitrogen, and metals in such a way that the heavy and/or extra-heavy crude oil can be transported to maritime terminals or to refining centers. The operation of the process at low severity conditions causes the catalyst to have long life thus reducing investment costs by diminishing the consumption of utilities. The obtained upgraded oils can be stored or transported directly to maritime terminals or to existing refineries, because their transport properties such as viscosity and API gravity are similar to those of light and medium crude oils usually processed. The combination of the type of reactor, type of catalyst and low severity conditions make the reactions to be oriented towards the hydrocracking, thus decreasing the selectivity to the removal of impurities, therefore the production of by-products is controlled, such as hydrogen sulfide, and the sweetening of produced gases is avoided, making the process more compact and simple.

EXAMPLES

(22) 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

(23) A heavy crude oil with 12.70 API and other properties presented in Table 1, was subjected to step 1) Desalting of heavy or extra-heavy crude oil of the present invention, to obtain a desalted crude oil with salt content lower than 1 ppm, with the same properties reported in Table 1.

(24) The desalted crude oil was subjected to stage 2) Catalytic hydrotreating of heavy and/or extra-heavy desalted crude oil of the present invention, using a single fixed-bed reactor at operating conditions given in Table 2.

(25) TABLE-US-00001 TABLE 1 Properties of heavy crude oil used as feedstock in all examples of the present invention. Properties Value Specific gravity 60/60 F. 0.9813 Specific weight 20/4 C. 0.9785 API Gravity 12.70 Kinematic viscosity, cSt @: 25.0 C. 17547 37.8 C. 4623 54.4 C. 1226 TBP Distillation, C. IBP/5 vol % 36/135 10/20 vol % 193/290 30/40 vol % 382/461 50/60 vol % 535/ 70/80 vol % / Conradson carbon, weight % 18.48 Sulfur, weight % 5.25 Total acid number (TAN), mg KOH/g 0.36 n-heptane-insolubles, weight % 17.34 Toluene-insolubles, weight % 0.30 Metals, wppm Nickel 85.59 Vanadium 456.23 Ni + V 541.82 IBP: Initial Boiling Point; TBP: True Boiling Point

(26) TABLE-US-00002 TABLE 2 Operating conditions of step 2) Catalytic hydrotreating of the desalted heavy and/or extra-heavy desalted crude oil, of the present invention, Example 1. Variable Condition Pressure, kg/cm.sup.2 50 Temperature, C. 385 Space velocity (LHSV), h.sup.1 0.25 H.sub.2/HC ratio, feet.sup.3/bbl 5,000

(27) The catalyst employed in Example 1 and all other examples of the present invention, has the properties shown in Table 3.

(28) TABLE-US-00003 TABLE 3 Properties of the catalyst, used in all examples of the present invention. Property Value Molybdenum, weight % 2.2 Nickel, weight % 0.6 Specific surface area, m.sup.2/g 199 Total pore volume, m.sup.2/g 0.85 Compact density, g/ml 0.584 Particle diameter, mm 1.15

(29) The catalytically hydrotreated product was subjected to Step 3) Separation of partially upgraded oil, of the present invention. The properties of the final product are reported in Table 4.

(30) From Table 4 it is important to note the considerable decrease in kinematic viscosity at 37.8 C. of heavy crude oil from 4623 cSt (Table 1) to 230.2 cSt in the partially upgraded oil (Table 4), which ensures compliance with the specification for transportation, which is equal to or less than 250 cSt measured at 37.8 C. The API gravity of heavy crude oil increased 4.68 degrees (from 12.7 to 17.38 API) helping the crude oil achieve better quality for transportation. The operating conditions of this processing allow for low sulfur removal from 5.25 weight % to 3.243 weight %. Low metal (Ni+V) removal is also obtained from a value of 541.82 ppm to 348.47 ppm. The sediment content shows low values of 0.012 weight %.

(31) TABLE-US-00004 TABLE 4 Properties of the partially upgraded oil (Example 1). Properties Value Specific gravity 60/60 F. 0.9504 Specific weight 20/4 C. 0.9476 API Gravity 17.38 Kinematic viscosity, cSt @: 25.0 C. 601.4 37.8 C. 230.2 54.4 C. 85.2 TBP Distillation, C. IBP/5 vol % 41/125 10/20 vol % 176/262 30/40 vol % 333/401 50/60 vol % 470/536 70/80 vol % / Sulfur, weight % 3.243 Metals, wppm Nickel 70.18 Vanadium 278.29 Ni + V 348.47 Sediment content, weight % 0.012 Conversion, vol %. 18.3 IBP: Initial Boiling Point; TBP: True Boiling Point

Example 2

(32) The desalted crude oil, obtained in step 1) of Example 1 was subjected to Step 2) catalytic hydrotreatment of heavy and/or extra-heavy desalted crude oil, process of the present invention, using a single fixed-bed reactor at operating conditions listed in Table 5.

(33) TABLE-US-00005 TABLE 5 Operating conditions of step 2) Catalytic hydrotreating of the heavy and/or extra-heavy crude oil, of the present invention, (Example 2). Variable Condition Pressure, kg/cm.sup.2 100 Temperature, C. 380 Space velocity (LHSV) 0.25 H.sub.2/HC ratio, feet.sup.3/bbl 5,000

(34) The catalytically hydrotreated product, was subjected to Step 3) Separation of partially upgraded crude, of the present invention, obtaining the final product whose properties are reported in Table 6.

(35) From Table 6, it is important to notice the significant decrease in kinematic viscosity at 37.8 C. of heavy crude oil, from 4,623 cSt (Table 1) to 151.0 cSt in the partially upgraded oil (Table 6), which far exceeds compliance with the specification for transportation; that is, a value equal to or less than 250 cSt measured at 37.8 C. The API gravity of heavy crude oil increased 8.02 degrees, from 12.7 to 20.72 API, helping substantially improve their quality for transport. The sulfur removal was carried out from 5.25 weight % to 1.95 weight %, which corresponds to a low removal level for this impurity. Metal removal obtained was from a value of 541.82 ppm Ni+V to a value of 185.9 ppm Ni+V. Finally, the sediment content displayed low values of 0011% wt.

(36) TABLE-US-00006 TABLE 6 Properties of partially upgraded oil (Example 2). Properties Value Specific gravity 60/60 F. 0.9296 Specific weight 20/4 C. 0.9268 API Gravity 20.72 Kinematic viscosity, cSt @: 37.8 C. 151.0 TBP Distillation, C. IBP/5 vol % 77/153.6 10/20 vol % 201.6/272.0 30/40 vol % 326.9/381.9 50/60 vol % 435.1/498.6 70/80 vol % 559.8/607.1 90/95 vol % 656.1/684.5 FBP 712.2 Sulfur, weight % 1.95 Metals, wppm Nickel 34.7 Vanadium 151.2 Ni + V 185.9 Sediment content, weight % 0.011 Conversion, vol %. 24.39 IBP: Initial Boiling Point; FBP: Final Boiling Point TBP: True Boiling Point

Example 3

(37) The catalytically hydrotreated product obtained from step 1) of Example 1, was also subjected to Step 2) Catalytic hydrotreating of heavy and/or extra-heavy desalted crude oil, of the present invention, using a single fixed-reactor at operating conditions given in Table 7.

(38) TABLE-US-00007 TABLE 7 Operating conditions of step 2) Catalytic hydrotreating heavy and/or extra-heavy desalted crude oil, of the present invention, of Example 3. Variable Condition Pressure, kg/cm.sup.2 100 Temperature, C. 390 Space velocity (LHSV), h.sup.1 0.5 H.sub.2/HC ratio, feet.sup.3/bbl 5,000

(39) The catalytically hydrotreated product was subjected to Step 3) Separation of partially upgraded oil, of the present invention, obtaining the final product whose properties are reported in Table 8.

(40) From Table 8 it is observed a decrease in the kinematic viscosity at 37.8 C. of heavy crude oil from 4623 cSt (Table 1) to 235.5 cSt in the partially upgraded product (Table 8), which also achieves the specification for its transportation, that is equal to or less than 250 cSt measured at 37.8 C. The API gravity of heavy crude oil increased 6.36 degrees, from 12.7 to 19.06 API, which improves the quality for its transportation. The sulfur removal in this case was from 5.25 weight % to 2.38 weight % which corresponds to a low level conversion of this impurity. Metal removal is obtained from 541.82 ppm Ni+V to 267.9 ppm. The sediment content offered low values of 0.009 weight %.

(41) TABLE-US-00008 TABLE 8 Properties of partially upgraded oil (Example 3). Properties Value Specific gravity 60/60 F. 0.9398 Specific weight 20/4 C. 0.9370 API Gravity 19.06 Kinematic viscosity, cSt @: 37.8 C. 235.5 TBP Distillation, C. IBP/5 vol % 75.3/149.5 10/20 vol % 207.6/288.9 30/40 vol % 348.4/403.9 50/60 vol % 458.1/520.3 70/80 vol % 578.8/629.0 90/95 vol % 673.1/694.2 FBP 716.2 Sulfur, weight % 2.38 Metals, wppm Nickel 56.1 Vanadium 211.8 Ni + V 267.9 Sediment content, weight % 0.009 Conversion, vol %. 18.53 IBP: Initial Boiling Point; FBP: Final Boiling Point; TBP: True Boiling Point

Example 4

(42) The desalted crude oil obtained from step 1) of Example 1, was further subjected to Step 2) Catalytic hydrotreating of heavy and/or extra-heavy crude oil, of the present invention, using a single fixed-bed reactor at operating conditions shown on Table 9.

(43) TABLE-US-00009 TABLE 9 Operating conditions of step 2) Catalytic hydrotreating of heavy and/or extra-heavy desalted crude oil, of the present invention, obtained in step 1 (Example 4). Variable Condition Pressure, kg/cm.sup.2 70 Temperature, C. 380 Space velocity (LHSV), h.sup.1 0.25 H.sub.2/HC ratio, feet.sup.3/bbl 5,000

(44) The catalytically hydrotreated product was subjected to Step 3) Separation of partially upgraded oil, of the present invention, obtaining the final product whose properties are detailed in Table 10.

(45) From Table 10 it is seen that the kinematic viscosity at 37.8 C. of heavy crude oil decreases from 4623 cSt (Table 1) to 192.0 cSt in the partially upgraded product (Table 10), which surpasses 250 cSt at 37.8 C., the specification for its transportation. The API gravity of heavy crude oil increased 6.59 degrees, from 12.7 to 19.29 API, contributing to improve the quality for its transportation. The sulfur content was reduced from 5.25 weight % to 2.22 weight %, maintaining a low level remotion for this impurity. Low metal removal is obtained from 541.82 ppm Ni+V to 245.5 ppm. The sediment content offered low values of 0.009 weight %.

(46) TABLE-US-00010 TABLE 10 Properties of partially upgraded oil (Example 4). Properties Value Specific gravity 60/60 F. 0.9384 Specific weight 20/4 C. 0.9356 API Gravity 19.29 Kinematic viscosity, cSt @: 37.8 C. 192.0 TBP Distillation, C. IBP/5 vol % 68.1/90.9 10/20 vol % 159.8/246.1 30/40 vol % 306.6/363.9 50/60 vol % 419.3/484.4 70/80 vol % 550.2/600.0 90/95 vol % 652.0/682.6 FBP 712.6 Sulfur, weight % 2.22 Metals, wppm Nickel 48.27 Vanadium 197.25 Ni + V 245.5 Sediment content, weight % 0.009 Conversion, vol %. 19.40 IBP: Initial Boiling Point; FBP: Final Boiling Point; TBP: True Boiling Point

Example 5

(47) The desalted heavy crude oil of Example 1 was subjected to step 2) Catalytic hydrotreating of heavy and/or extra-heavy desalted crude oil, of the present invention, using a single fixed-bed reactor at operating conditions given in Table 11.

(48) TABLE-US-00011 TABLE 11 Operating conditions of step 2) Catalytic hydrotreating of heavy and/or extra-heavy desalted crude oil, of the present invention, (Example 5). Variable Condition Pressure, kg/cm.sup.2 50 Temperature, C. 390 Space velocity (LHSV), h.sup.1 0.25 H.sub.2/HC ratio, feet.sup.3/bbl 5,000

(49) The catalytically hydrotreated product was subjected to Step 3) Separation of partially upgraded oil of the present invention, obtaining the final product whose properties are reported in Table 12.

(50) The kinematic viscosity at 37.8 C. of heavy crude oil is reduced from 4623 cSt (Table 1) to 173.5 cSt in the partially upgraded product (Table 12), which also achieves the specification for its transportation, that is equal to or less than 250 cSt measured at 37.8 C. The API gravity of heavy crude oil increased 5.95 degrees from 12.7 to 18.65 API. The sulfur removal was from 5.25 weight % to 2.84 weight %. Metal removal is obtained from 541.82 ppm to 291.8 ppm Ni+V. The sediment content presented low values of 0.029 weight %.

(51) TABLE-US-00012 TABLE 12 Properties of partially upgraded oil (Example 5). Properties Value Specific gravity 60/60 F. 0.9424 Specific weight 20/4 C. 0.9396 API Gravity 18.65 Kinematic viscosity, cSt @: 37.8 C. 173.3 TBP Distillation, C. IBP/5 vol % 97.2/173.3 10/20 vol % 228.1/293.1 30/40 vol % 346.4/398.2 50/60 vol % 448.7/506.7 70/80 vol % 567.3/625.3 90/95 vol % 672.0/693.6 FBP 716.5 Sulfur, weight % 2.84 Metals, wppm Nickel 59.8 Vanadium 232.0 Ni + V 291.8 Sediment content, weight % 0.029 Conversion, vol %. 24.15 IBP: Initial Boiling Point; FBP: Final Boiling Point; TBP: True Boiling Point

Example 6

(52) The desalted crude oil obtained from step 1) of Example 1, was further subjected to Step 2) Catalytic hydrotreating of heavy and/or extra-heavy desalted crude oil of the present invention, using a single fixed reactor at operating conditions shown on Table 13.

(53) TABLE-US-00013 TABLE 13 Operating conditions of step 2) Catalytic hydrotreating of the heavy and/or extra-heavy desalted crude oil, (Example 6). Variable Condition Pressure, kg/cm.sup.2 50 Temperature, C. 400 Space velocity (LHSV), h.sup.1 0.5 H.sub.2/HC ratio, feet.sup.3/bbl 5,000

(54) The catalytically hydrotreated product was subjected to Step 3) Separation of upgraded oil for its transportation of the present invention, obtaining the final product whose properties are shown in Table 14.

(55) From Table 14 it is important to remark the decrease in the kinematic viscosity at 37.8 C. of heavy crude oil from 4623 cSt (Table 1) to 221.1 cSt in the partially upgraded product (Table 11), which also achieves the specification for its transportation, that is equal to or less than 250 cSt measured at 37.8 C. The API gravity of heavy crude oil increased 4.61 degrees from 12.7 to 17.31 API. The sulfur removal was from 5.25 weight % to 3.5 weight %. Low metal (Ni+V) removal is obtained from 541.82 ppm to 417.1 ppm. Finally, the corresponding sediment content was 0.036 weight %.

(56) TABLE-US-00014 TABLE 14 Properties of partially upgraded oil (Example 6). Properties Value Specific gravity 60/60 F. 0.9509 Specific weight 20/4 C. 0.9481 API Gravity 17.31 Kinematic viscosity, cSt @: 37.8 C. 221.1 TBP Distillation, C. IBP/5 vol % 94.9/169.7 10/20 vol % 220.2/292.6 30/40 vol % 350.6/407.4 50/60 vol % 462.5/519.4 70/80 vol % 567.7/616.2 90/95 vol % 666.4/691.0 FBP 715.7 Sulfur, weight % 3.50 Metals, wppm Nickel 75.9 Vanadium 341.2 Ni + V 417.1 Sediment content, weight % 0.036 Conversion, vol %. 21.95 IBP: Initial Boiling Point; FBP: Final Boiling Point; TBP: True Boiling Point

(57) From the results of the tables of the above examples it is important to highlight the significant decrease in kinematic viscosity at 37.8 C. of heavy crude oil from 4623 cSt (Table 1) to values in the partially upgraded oil that achieve the specification for transportation, that is equal to or less than 250 cSt at 37.8 C. The API gravity of heavy crude oil shows increments of 4.61-8.02 degrees making the crude oil to have better quality for transportation. The operating conditions of the process of this invention allow for sulfur removal from 5.25 weight % to 1.95 weight %, which does not produce excessive amount of hydrogen sulfide and hence does not require additional equipment for the treating of sour gas. The low metal removal (Ni+V) is performed from 541.82 ppm to 185.9 ppm, with these data and considering the hydrocarbon mass entering and leaving the reactor, a mass balance is performed to estimate the amount of metals deposited on the catalyst surface by means of difference, which is divided by the amount of catalyst loaded to the reactor, and thereby the rate of metal deposition on the catalyst is determined.

(58) The metal deposition rate on the catalyst is calculated by dividing the percentage of metal deposit (weight %) over the accumulated time-on-stream in hours to obtain a deposition rate, which was found to be 0.0168 weight % per hour. This deposition rate allows to calculate the lifetime of the catalyst by dividing the maximum metal retention capacity of the catalyst (120 weight % for this catalyst) over the metal deposition rate (in weight %/h), resulting in 10 months approximately.

(59) The metal deposition rate is not influenced by the change of operating conditions so this value is the same for all examples of the present invention.

(60) In addition, the sediment content shows low levels lower than 0.04 weight %, allowing the process to be maintained for long operating cycles.