MXPA06006795A

MXPA06006795A - Systems, methods, and catalysts for producing a crude product.

Info

Publication number: MXPA06006795A
Application number: MXPA06006795A
Authority: MX
Inventors: Opinder Kishan Bhan
Original assignee: Shell Int Research
Priority date: 2003-12-19
Filing date: 2004-12-16
Publication date: 2006-08-23
Also published as: CA2551091C; AU2004312365A1; BRPI0405537B1; TW200535223A; NL1027753A1; KR20070032625A; NL1027769C2; WO2005063927A2; CA2549873A1; JP2007514835A; WO2005066303A2; EP1702047A2; EP1713886A2; TW200530387A; NL1027752A1; JP2007514849A; CA2548914C; EP1713887A2; BRPI0405568B1; BRPI0405570B1

Abstract

Contact of a crude feed with one or more catalysts produces a total product that include a crude product. The crude product is a liquid mixture at 25 degree C and 0.101 MPa. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Description

SYSTEMS, METHODS AND CATALYSTS TO PRODUCE A CRUDE PRODUCT FIELD OF THE INVENTION The present invention generally relates to systems, methods and catalysts for the treatment of a crude feed, and to compositions that can be produced using such systems, methods and catalysts. More particularly, certain embodiments described herein are refer to systems, methods and catalysts used for the conversion of a crude feed to a total product, where the total product includes a crude product that is a liquid mixture at 25 ° C and 0.101 MPa and that contains one or more properties that they are changed in relation to the respective property of the crude feed.

BACKGROUND OF THE INVENTION Oil that can not be transported economically because it has one or more inadequate properties, or that can not be processed using conventional infrastructure, is commonly referred to as "crude bear-bear". The disntageous crude may include acid components that contribute to the total acid numerical content ("TAN") of the crude feed. REF. DO NOT. 173446 The disntageous crude oil with a relatively high TAN index can contribute to the corrosion of metallic components during transport and / or processing of crude oil bear. The removal of acidic components from the disntageous crude can include the chemical neutralization of the acid components with various bases. Alternatively, corrosion-resistant metals can be used in the transport equipment and / or in the processing equipment. The use of corrosion-resistant metals generally involves a significant expense, and therefore, it is desirable to avoid the use of these corrosion-resistant metals in existing equipment. Another method to inhibit corrosion may include adding corrosion inhibitors to the crude oil, prior to transport and / or processing thereof. The use of corrosion inhibitors can negatively affect the equipment used for the processing of crude oils, or the quality of products obtained from crude oil. The disntageous crude usually contains relatively high levels of residue. High levels of waste tend to raise the cost of transportation and / or processing with conventional infrastructure. The disntageous crude usually contains organically bound heteroatoms (for example, sulfur, oxygen and nitrogen). The organically bound heteroatoms can sometimes produce rse effects on the catalysts. The disntageous crude may include relatively high amounts of polluting metals, for example, nickel, vanadium and / or iron. During the processing of this crude, contaminating metals and / or compounds with polluting metals can be deposited on the catalyst surface or in the empty volume of catalyst. This can make the catalyst less active. Coke can be formed, which can eventually deposit on the catalyst surfaces rapidly during processing of the disntageous crude. It can be expensive to regenerate the catalytic activity of a catalyst that is contaminated with coke. In addition, the high temperatures used in the regeneration can decrease the activity of the catalyst and / or cause its deterioration. The disntageous crude may include metals in metal salts of organic acids (eg, calcium, potassium and / or sodium). It is not common for metals in metal salts of organic acids to be separated from the disntageous crude by conventional processes, for example, by desalting and / or acid washing. Processes are commonly described in conventional processes when they contain metals in metallic salts of organic acids. Contrary to what happens with nickel and vanadium, which are usually deposited next to the external surface of the catalyst, the metals in metal salts of organic acids can be deposited, preferably, in the empty volumes between the catalyst particles, particularly, on the upper surface of the catalyst bed. Depositing contaminants, such as, for example, metals in the metal salts of organic acids, on the upper surface of the catalyst bed generally produces an increase in the drop pressure across the bed and can effectively seal the catalyst bed. In addition, metals in metal salts of organic acids can cause a rapid deactivation of the catalysts. The disadvantageous crude may include organic oxygen compounds. It is possible that the infrastructure used for the treatment, in which the disadvantageous crude is processed with an oxygen content of at least 0.002 grams of oxygen per gram of crude is disadvantageous, and may present problems during processing. Organic oxygen compounds can form higher oxidation compounds when heated during processing (eg ketones and / or acids formed by oxidation of alcohols, and / or acids formed by the oxidation of ethers) which are difficult to remove from the crude treated and / or can produce either corrosion or contamination of the equipment during processing, and can cause the shutdown of transport lines. The disadvantageous crude may include hydrocarbons without hydrogen. During the processing of hydrocarbons without hydrogen, it is generally necessary to add consistent amounts of hydrogen, particularly if unsaturated fragments are produced due to cracking processes. Hydrogenation may be necessary during processing, which generally involves the use of an active hydrogenation catalyst, such that the formation of carbon from unsaturated fragments is inhibited. It is expensive to produce and / or transport the hydrogen for the treatment of the infrastructure. In addition, unfavorable crude tends to be unstable during processing when conventional infrastructure is used. The instability of the crude tends to cause the phases of the components to separate during the processing and / or formation of unwanted by-products (eg, hydrogen sulfide, water, and carbon dioxide). In general, by means of conventional processing it is not possible to significantly change another of the disadvantageous crude properties. For example, by conventional processes it is usually not possible to reduce the TAN index of a disadvantageous crude oil and at the same time change only the desired quantity of a certain component of the disadvantageous crude (for example, sulfur or polluting metals). Some processes that are applied to improve the quality of the crude oil include the addition of a diluent to the disadvantageous crude to decrease the percentage by weight of the components that are some of the determinants of the unfavorable properties of the crude oil. However, the addition of diluent increases the costs associated with the treatment of disadvantageous crude oil, the cost of diluents and / or increase the costs incurred when handling unfavorable crude oil. When adding to a crude disadvantageous diluent it can in certain situations cause the loss of stability of the crude oil. U.S. Pat. Nos. 6,547,957 of Sudha ar et al.; 6,277,269 of Meyers 6,063,266 of Grande et al .; 5,928,502 to Bearden et al; 5,914,030 to Bearden et al; 5,897,769 to Trachte et al .; 5,871,636 to Trachte et al .; and 5,851,381 to Tanaka et al. describe various processes, systems and catalysts used in the processing of crude oil. However, due to the aforementioned technical problems, the processes, systems, catalysts described in these patents are of limited application.

In conclusion, generally disadvantageous crude has undesired properties (for example, its TAN index is relatively high, a tendency to destabilize during treatment, and / or tend to consume large amounts of hydrogen during treatment). Other undesired properties include relatively high concentrations of unwanted components (eg, residues, organically bound heteroatoms, polluting metals, metals in metal salts of organic acids, and / or compounds with organic oxygen). Such properties give rise to complications and / or in conventional transport or in the treatment infrastructure, including increased corrosion, a decrease in catalyst half-life, clogging or even greater use of hydrogen during treatment. Therefore, it is very necessary, from the economic and technical point of view, to have better systems, methods or catalysts to convert the disadvantageous crude oil products that have more desirable properties. It is also very necessary from the economic and technical point of view to have systems, methods and / or catalysts that can change the properties that are selected in the disadvantageous crude without changing the other properties of the same.

BRIEF DESCRIPTION OF THE INVENTION In general terms, the inventions described herein describe systems, methods and catalysts used in the conversion of a crude feed into a total product, including the crude product, and in some aspects, also a gas not condensable. In addition, the inventions described herein generally define compositions with new combinations of components thereof. Such compositions are produced using such systems and methods described herein. The invention provides a method for producing a crude product comprising: contacting a crude feed with one or more catalysts, to produce a total product including the crude product, wherein the crude product is a liquid mixture at 25 ° C. and 0.10 1 MPa, the crude feed in turn has a TAN index of at least 0.3, and at least one of the catalysts has a pore size distribution with a mean pore diameter in the range of 90 A to 180 A, with minus 60% of the total number of pores in the distribution with a pore diameter within 45 A of the average pore diameter; where the pore size distribution is determined with the method ASTM D4282; and at the same time controlling the conditions of contact, so that the raw product has a TAN index of not more than 90% of the TAN index of the crude feed, where the TAN index is determined in turn with the method ASTM D664. "The invention also provides a method for producing a crude product comprising: contacting the crude feed with one or more catalysts, to obtain a total product that includes the crude product, wherein the raw product is a mixture liquid at 25 ° C and 0.101 MPa, the crude feed has a TAN index of at least 0.3, at least one of the catalysts has a pore size distribution with a mean-pore diameter of at least 90 A, determined by the ASTM method D4282, and the catalyst has a pore size distribution that has, per gram of catalyst, 0.0001 to 0.08 grams of: molybdenum, one or more "molybdenum compounds, which are calculated as molybdenum weight, or the mixture thereof; and controlling contact conditions such that the crude product has a TAN index of no more than 90% of the same crude feed index, where the TAN index is as determined by the ASTM D664 method. The invention also provides a method for producing a crude product comprising: contacting a crude feed with one or more catalysts, to produce a total product that includes the crude product, where the crude product is a liquid mixture at 25 ° C. and 0.101 MPa, the crude feed has a TAN index of at least 0.3, as determined by ASTM D644, at least one of the catalysts has a pore size distribution with a mean pore diameter of at least 180 A, determined by the ASTM method D4282, and the catalyst has a pore size distribution comprising one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of said table, or mixtures of the same; and to control the contact conditions, such that the raw product contains a TAN index of at least 90% of the referred index of the crude feed, the TAN index is determined by the ASTM D664 method. The invention also provides a method for producing a crude product comprising: contacting the crude feed with one or more catalysts, to produce a total product including the crude product, where the crude product is a liquid mixture at 25 ° C. and 0.101 MPa, the crude feed has a TAN index of at least 0.3, determined by the ASTM D664 method, and at least one of the catalysts comprises: (a) one or more metals from Column 6 of the Periodic Table, one or more compounds of one or more metals of Column 6 of the Periodic Table, or mixtures thereof; and (b) one or more metals of a Column 10 of the Periodic Table, one or more compounds of one or more metals of Column 10 of the Periodic Table, or mixtures thereof, and wherein the molar ratio between all the metal of column 10 and all the metal of column 6 is in the range of 1 to 10; and control the contact conditions, such that the raw product has a TAN index of not more than 90% of the TAN index of the crude feed, where the TAN index is determined by the ASTM D664 method. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts, to produce a total product including the crude product, wherein the raw product is a liquid mixture at 25%. ° C and 0.101 MPa, the crude feed has a TAN index of at least 0.3, and one or more of the catalysts comprises: (a) a first catalyst, which has, per gram thereof, from 0.0001 to 0.06 grams of: one or more metals of Column 6 of the Periodic Table, one or more compounds of one or more metals of column 6 of the Periodic Table, calculated as metal weight, or their mixtures; and (b) a second catalyst, which has, per gram of the second catalyst, at least 0.02 grams of: one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, calculated as weight of metal, or their mixtures; and controlling contact conditions such that the crude product has a TAN index of not more than 90% of the same crude feed index, where the TAN index is as determined by the ASTM D664 method. The invention also provides a catalyst composition, comprising: (a) one or more metals from column 5 of the Periodic Table, one or more compounds from one or more metals from column 5 of the Periodic Table, or mixtures thereof. same; (b) a base material having theta alum content of at least 0.1 gram of theta alumina per gram of base material, as determined by x-ray diffraction; and wherein the catalyst has a pore size distribution with a mean pore diameter of at least 230A, as determined by the ASTM method D4282. The invention also provides a catalyst composition, comprising: (a) one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof same; (b) a base material having theta alum content of at least 0.1 gram of theta alumina per gram of base material, as determined by x-ray diffraction; and wherein the catalyst has a pore size distribution with an average pore diameter of at least 230 A, as determined by the ASTM method D4282. The invention further provides a catalyst composition, comprising: (a) one or more metals from column 5 of the Periodic Table, one or more compounds from one or more metals from column 5 of the Periodic Table, one or more metals from column 6 of the Periodic Table, one or more compounds of one or more metals from column 6 of the Periodic Table, or mixtures thereof; (b) a base material having theta alum content of at least 0.1 gram of theta alumina per gram of base material, as determined by x-ray diffraction; and wherein the catalyst has a pore size distribution with a mean pore diameter of at least 230A, as determined by the ASTM method D4282. The invention also provides a method for producing a catalyst comprising: combining a base with one or more metals to form a base / metal mixture, wherein the base comprises theta alumina, and one or more of the metals comprising one or more metals from column 5 of the Periodic Table, one or more compounds from one or more metals from column 5 of the Periodic Table, or mixtures thereof; heat treating the theta alumina / metal base mixture at a temperature of at least 400 ° C; and forming the catalyst, wherein which has a pore size distribution with a mean pore diameter of at least 230 A, as determined by the ASTM method D4282. The invention also provides a method for producing a catalyst, comprising: combining a base with one or more metals to form a base / metal mixture, wherein the base comprises theta alumina, and one or more of the metals comprising one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof; heat treating theta alumina / metal base mixture at a temperature of at least 400 ° C; and forming the catalyst, wherein the catalyst has a pore size distribution with a mean pore diameter of at least 230 A, as determined by the ASTM method D4282. The invention also provides a method for producing a crude product, comprising: contacting the crude source with one or more catalysts to obtain a total product including the crude product, wherein the crude product is a liquid mixture at 25 ° C. and 0.101 MPa, the crude feed has a TAN index of at least 0.3, at least one of the catalysts has a pore size distribution with a mean pore diameter of at least 180 Á, as determined by the ASTM method D4282 , and the catalyst has the pore size distribution comprising theta alumina and one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof. the same; and controlling contact conditions such that the crude product has a TAN index of not more than 90% of the TAN index of the crude feed, where the TAN index is as determined by the ASTM D664 method. The invention also provides a method for producing a crude product, comprising: contacting the crude feed with one or more catalysts in the presence of a source of hydrogen to obtain a total product including the crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.10 1 MPa, the crude feed has a TAN index of at least 0.3, the crude feed has an oxygen content of at least 0.0001 grams of oxygen per gram of crude feed, and at least one of the catalysts has a pore size distribution with a mean pore diameter of at least 90 A, as determined by the ASTM method D4282; and controlling contact conditions to decrease the TAN index such that the raw product has a TAN index of not more than 90% of the TAN index of the crude feed, and to reduce the organic oxygen content contained in the compounds such that the raw product has an oxygen content of not more than 90% of the oxygen content of the crude feed, where the TAN index is as determined by the ASTM D664 method, and the oxygen content is as determined by the method ASTM E385. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to obtain a total product including the crude product, where the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the crude feed has a TAN index of at least 0.1, and at least one of the catalysts has for each gram of catalyst, at least 0.001 grams of : one or more metals of column 6 of the Periodic Table, one or more compounds of one or more metals of column 6 of the Periodic Table, calculated as the weight of the metal, or their mixtures; and controlling contact conditions such that the liquid space velocity per hour in a contact zone is greater than 10 h "1, and the crude product has a TAN index of not more than 90% of the TAN index of the crude feed , wherein the TAN index is as determined by the ASTM method D664 The invention also provides a method for producing a crude product, comprising: contacting the crude feed with one or more catalysts in the presence of a hydrogen source for obtain a total product that includes the crude product, where the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the crude feed has a TAN index of at least 0.1, the crude feed has a sulfur content of at least 0.0001 grams of sulfur per gram of crude feed, and at least one of the catalysts comprises one or more metals from column 6 of the Periodic Table, one or more compounds of one or more metals of the lumna 6 of the Periodic Table, or their mixtures; and controlling contact conditions such that, during contact, the crude feed absorbs the molecular hydrogen at a selected rate to inhibit the phase separation of the source of curd during contact, the spatial velocity of liquid per hour in one or more contact zones is greater than 10 h "1, the crude product has a TAN index of no more than 90% of the TAN index of the crude feed, and the raw product has a sulfur content of 70-130% of the content of sulfur from the crude feed, where the TAN index is as determined by the ASTM method D664, and the sulfur content is as determined by the ASTM method D4294.The invention also provides a method for producing a crude product, which comprises: contacting the crude feed with one or more catalysts in the presence of a gaseous hydrogen source to produce a total product that includes the crude product, where the raw product is a liquid mixture at 25 ° C and 0.101 MPa; and controlling - the contact conditions such that the crude feed, during contact, absorbs the hydrogen at a selected rate to inhibit the separation of the phases of the crude feed during contact. The invention also provides a method for producing a crude product, comprising: contacting the crude feed with hydrogen in the presence of one or more catalysts to produce a total product including the crude product, wherein the crude product is a mixture liquid at 25 ° C and 0.101 MPa; and controlling contact conditions such that the crude feed is contacted with hydrogen in a first hydrogen absorption condition and then a second hydrogen absorption condition, the first hydrogen absorption condition is different from the second hydrogen hydrogen uptake, and the net hydrogen uptake in the first hydrogen uptake condition is contro to inhibit the P value of a crude feed / total product mixture from a decrease below 1.5 and one or more change properties crude product by more than 90% relative to one or more respective properties of the crude feed. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts at a first temperature followed by contact at a second temperature to obtain a total product including the crude product, where the crude product is a liquid mixture at 25 ° C to 0.101 MPa, the crude feed has a TAN index of at least 0.3; and controlling contact conditions such that the first contact temperature is at least 30 ° C lower than the second contact temperature, and the crude product has a TAN index of not more than 90% of the TAN index of the crude feed , where the TAN index is as determined by the ASTM D664 method. The invention also provides a method for producing a crude product, which comprises: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, where the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the crude feed has a TAN index of at least 0.3, the crude feed has a sulfur content of at least 0.0001 grams of sulfur per gram of crude feed, and at least one of the catalysts includes one or more metals from column 6 of the Periodic Table , one or more compounds of one or more metals from column 6 of the Periodic Table, or their mixtures; and control contact conditions, such that the raw product has a TAN index of not more than 90% of the TAN index of the crude feed, and the crude product has a sulfur content of 70-130% of the sulfur content of the crude feed, where the TAN index is as determined by the ASTM D664 method, and the sulfur content as determined by the ASTM D4294 method. The invention also provides a method for producing a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product including the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has a TAN index of at least 0.1, the crude feed has a residual content of at least 0.1 grams of the residue per gram of crude feed, and at least one of the catalysts comprises one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof; and control contact conditions, such that the raw product has a TAN index of not more than 90% of the TAN index of the crude feed, and the crude product has a residual content of 70-130% of the residual content of the feed of crude, where the TAN index is as determined by the ASTM D664 method, and the residual content is as determined by the ASTM D5307 method. The invention also provides a method for producing a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product including the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has a TAN index of at least 0.1, the crude feed has a VGO content of at least 0.1 grams of VGO per gram of crude feed, and at least one of the catalysts comprises one or more metals of column 6 of the Periodic Table, one or more compounds of one or more metals of column 6 of the Periodic Table, or mixtures thereof; and control contact conditions, such that the raw product has a TAN index of not more than 90% of the TAN index of the crude feed, and the raw product has a VGO content of 70-130% of the VGO content of the crude feed, and where the VGO content is as determined by the ASTM D5307 method. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has a TAN index of at least 0.3, and at least one of the catalysts is obtained by: the combination of a base with one or more metals from column 6 of the Periodic Table, one or more compounds of one or more metals from column 6 of the Periodic Table, or mixtures thereof, to produce a catalyst precursor; and forming the catalyst by heating the catalyst precursor in the presence of one or more sulfur-containing compounds at a temperature below 500 ° C; and control the contact conditions such that the raw product has a TAN index of not more than 90% of the TAN index of the crude feed.

The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25%. ° C and 0.101 MPa, the crude feed has a viscosity of at least 10 cST at 37.8 ° C (100 ° F), the crude feed has an API gravity of at least 10, and at least one of the catalysts comprises one or more metals of column 6 of the Periodic Table, one or more compounds of one or more metals of column 6 of the Periodic Table, or mixtures thereof; and controlling contact conditions, such that the raw product has a viscosity at 37.8 ° C of no more than 90% of the viscosity of the crude feed at 37.8 ° C, and the crude product has an API gravity of 70-130. % of API gravity of crude feed, where API gravity is as determined by ASTM method D6822, and viscosity is as determined by ASTM method D2669. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has a TAN index of at least 0.1, and at least one of the catalysts comprises: at least one catalyst comprising vanadium, one or more vanadium compounds, or mixtures thereof, and an additional catalyst , wherein the additional catalyst comprises one or more metals from column 6, one or more compounds from one or more metals from column 6, or combinations thereof; and controlling contact conditions such that the crude product has a TAN index of not more than 90% of the TAN index of the crude feed, the TAN index is as determined by the ASTM D664 method. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, where the crude product is a liquid mixture at 25 ° C. and 0.101 MPa, and the crude feed has a TAN index of at least 0.1; generate hydrogen during contact; and controlling contact conditions such that the crude product has a TAN index of not more than 90% of the TAN index of the crude feed, where the TAN index is as determined by the ASTM D664 method. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, where the crude product is a liquid mixture at 25 ° C. and 0.101 MPa, and the crude feed has a TAN index of at least 0.1; and at least one of the catalysts comprises vanadium, one or more vanadium compounds, or mixtures thereof; and controlling contact conditions such that the contact temperature is at least 200 ° C, and the crude-product has a TAN index of not more than 90% of the TAN index of the crude feed, where the TAN index is as determined by the method ASTM D664. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, where the crude product is a liquid mixture at 25 ° C. and 0.101 MPa, and the crude feed has a TAN index of at least 0.1; and at least one of the catalysts comprises vanadium, one or more vanadium compounds, or mixtures thereof; providing a gas comprising a source of hydrogen during contact, the gas flow being supplied in a direction opposite to the flow of the crude feed; and control contact conditions such that the raw product has a TAN index of not more than 90% of the TAN index of the crude feed, where the TAN index is as determined by the ASTM D664 method. The invention also provides a method for obtaining a crude product, comprising: contacting the crude source with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed contains, per gram of crude feed, a total Ni / V / Fe content of at least 0.00002 grams, at least one of the catalysts comprises vanadium, one or more vanadium compounds, or their mixtures, and the vanadium catalysts have a pore size distribution with a mean pore diameter of at least 180 A; and controlling contact conditions such that the crude product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, the Ni / V / Fe content is as determined by the method ASTM D5708. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalyto obtain the total product that includes the crude product, wherein the raw product is a liquid mixture at 25 °. C and 0.101 MPa, at least one of the catalycomprises vanadium, one or more vanadium compounds, or mixtures thereof, the crude feed comprises one or more alkali metal salts of one or more organic acids, one or more salts of metals alkaline earths of one or more organic acids or their mixtures, and the crude feed has per gram of crude feed, a total content of alkali metal and alkaline earth metal in metal salts of organic acids of at least 0.00001 grams; and controlling contact conditions such that the crude product has a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of not more than 90% of the content of the alkali metal, and alkaline earth metal, in metal salts of organic acids in the crude feed, wherein the content of alkali metal, and alkaline earth metal in metal salts of organic acids is determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting a crude feed with one or more catalyto obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, the crude feed has per gram of crude feed, a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.00001 grams, and at least one of the catalyhas a pore size distribution with a mean pore diameter in the range from 90 Á to 180 Á, with at least 60% of the total number of pores in the pore size distribution having a pore diameter within 45 A of the diameter of or medium, where the pore size distribution is as determined by the ASTM method D4282; and controlling contact conditions such that the crude product has a total content of alkali metal, alkaline earth metal in metal salts of organic acids of not more than 90% of the alkali metal content, and alkaline earth metal, in metal salts of organic acids of the crude feed, where the content of alkali metal, alkaline earth metal, in metal salts of organic acids is as determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting a crude feed with one or more catalyto obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has, per gram of crude feed, a total Ni / V / Fe content of at least 0.00002 grams, and at least one of the catalyhas a pore size distribution with a diameter of average pore in the range of 90 Á to 180 A, with at least 60% of the total number of pores in the pore size distribution having a pore diameter within 45 Á of the average pore diameter, where the size distribution of pore is as determined by the method ASTM D4282; and controlling contact conditions such that the crude product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, where Ni / V / Fe is like it is determined by the method ASTM D5708. The invention also provides a method for obtaining a crude product, which comprises: contacting a crude feed with one or more catalysts to obtain a total product that includes the crude product, where the raw product is a liquid mixture at 25 ° C and 0.101 MPa, the crude feed has a total content of alkali metals, and alkaline earth metals, in metal salts of organic acids of at least 0.00001 grams per gram of crude feed, at least one of the catalysts has a pore size distribution with a mean pore diameter of at least 180A, as determined by the method ASTM D4282, and the catalyst has a pore size distribution comprising one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or their mixtures; and controlling the contact conditions such that the crude product has a total content of alkali metal, and alkaline earth metal in metal salts of organic acids of not more than 90% of the content of the alkali metal, and alkaline earth metal, in metal salts of organic acids in the crude feed, wherein the content of alkali metal, and alkaline earth metal in metal salts of organic acids is as determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed comprises one or more alkali metal salt of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, and the crude feed has per gram of crude feed, a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.00001 grams, and at least one of the catalysts has a pore size distribution with an average pore diameter of minus 230 A, as determined by the method ASTM D4282, and the catalyst has a pore size distribution comprising one or more metals from column 6 of Table P eriodic, one or more compounds of one or more metals from column 6 of the Periodic Table, or mixtures thereof; and controlling contact conditions such that the crude product has a total content of alkali metal, alkaline earth metal in metal salts of organic acids of not more than 90% of the alkali metal content, and an alkaline earth metal, in metal salts - of acids organic from the crude feed, wherein the content of alkali metal, alkaline earth metal in metal salts of organic acids is as determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting a crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has a total Ni / V / Fe content of at least 0.00002 grams per Ni / V / Fe per gram of crude feed, at least one of the catalysts has a pore size distribution with a mean pore diameter of at least 230A, as determined by the method ASTM D4282, and the catalyst has a pore size distribution comprising one or more metals from column 6 of the Periodic Table, one or more compounds of one or more metals from column 6 of the Periodic Table, or mixtures thereof; and controlling contact conditions such that the crude product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, where the Ni / V / Fe content it is as determined by the method ASTM D5708. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, the crude feed has a total content , per gram of crude feed, alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.00001 grams, at least one of the catalysts has a pore size distribution with a mean pore diameter of at least 90 Á, as determined by the method ASTM D4282, and the catalysts have the pore size distribution with a total molybdenum content, per gram of catalyzed or, from 0.0001 grams to 0.3 grams of: molybdenum, one or more molybdenum compounds, calculated as weight of molybdenum, or their mixtures; and controlling contact conditions such that the crude product has a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of not more than 90% of the alkali metal content, and alkaline earth metal, in metal salts of acids organic in the crude feed, wherein the content of alkali metal, and alkaline earth metal in metal salts of organic acids is as determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has a TAN index of at least 0.3 and the crude feed has, per gram of crude feed, a total content of Ni / V / Fe of at least 0.00002 grams, at least one of the catalysts have a pore size distribution with a mean pore diameter of at least 90 A, as determined by the method ASTM D4282, and the catalyst has a total molybdenum content, per gram of catalyst, from 0.0001 grams to 0.3 grams of: molybdenum, one or more molybdenum compounds, calculated as the weight of molybdenum, or mixtures thereof; and control contact conditions such that the crude product has a TAN index of not more than 90% of the TAN index of the crude feed and the crude product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, the Ni / V / Fe content is as determined by the ASTM D5708 method, and the TAN index is as determined by the ASTM D644 method. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, and the crude feed has a total content, per gram of crude feed, alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.00001 grams, and at least one of the catalysts comprises: (a) one or more metals from column 6 of the Periodic Table, one or more compounds of one or more metals from column 6 of the Periodic Table, or mixtures thereof; and (b) one or more metals from column 10 of the Periodic Table, one or more compounds from one or more metals from column 10 of the Periodic Table, or mixtures thereof, wherein a molar ratio of the total metal of the column 10 and column 6 is in the range of 1 to 10; and controlling contact conditions such that the crude product has a total content of alkali metal, and alkaline earth metal, in salts of organic acids of not more than 90% of the alkali metal content, and alkaline earth metal, in metal salts of organic acids in the crude feed, wherein the content of alkali metal, and alkaline earth metal, in metal salts of organic acids is as determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has a total Ni / V / Fe content of at least 0.00002 grams of Ni / V / Fe for each gram of crude feed, and at least one of the catalysts comprises: (a) one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or their mixtures; and (b) one or more metals from column 10 of the Periodic Table, one or more compounds from one or more metals from column 10 of the Periodic Table, or mixtures thereof, wherein the molar ratio of the total metal of the column 10 and column 6 is in the range of 1 to 10; and controlling contact conditions such that the crude product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, where the Ni / V / Fe content it is as determined by the method ASTM D5708. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, the crude feed has, per gram of crude feed, a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.00001 grams, and at least one of the catalysts comprise: (a) a first catalyst, the first catalyst has, for gram of the first catalyst, from 0.0001 to 0.06 grams of: one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the T Periodic abla, calculated as weight of metal, or their mixtures; and (b) a second catalyst, the second catalyst has, per gram of the second catalyst, at least 0.02 grams of: one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from the column 6 of the Periodic Table, calculated as metal weight, or their mixtures; and controlling contact conditions such that the crude product has a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of not more than 90% of the alkali metal content, and alkaline earth metal, in metal salts of acids organic in the crude feed, where the content of alkali metal, and alkaline earth metal in metal salts of organic acids is as determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting the raw feed "with one or more catalysts to obtain a total product that includes the crude product, wherein the raw product is a liquid mixture of 25 ° C and 0.101 MPa, the crude feed includes one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, the crude feed has, per gram of crude feed, a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.00001 grams, and at least one of the catalysts has, per gram of catalyst, at least 0.00 1 grams of : one or more metals of column 6 of the Periodic Table, one or more compounds of one or more metals of column 6 of the Periodic Table, calculated as weight of metal, or their mixtures, and control contact conditions such that the space velocity of liquid per hour in the contact zone exceeds 10 h "1, and the crude product has a total content of alkali metal, and alkaline earth metal, in metallic salts of organic acids of no more 90% of the content of alkali metal, and alkaline earth metal, in metal salts of organic acids in the crude feed, where the content of alkali metal, and alkaline earth metal in metal salts of organic acids is as determined by the method ASTM D1318 . The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, where the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the crude feed has a total content of Ni / V / Fe of at least 0.00002 grams and at least one of the catalysts has, per gram of catalyst , at least 0.001 grams of: one or more metals from column 6 of the Periodic Table of elements, one or more compounds of one or more metals from column 6 of the Periodic Table, calculated as weight of metal, or their mixtures; and controlling contact conditions such that the liquid space velocity per hour in a contact zone is greater than 10 bf1, and the crude product has a total Ni / V / Fe content of not more than 90% of the content of Ni / V / Fe of the crude feed, where the Ni / V / Fe content is as determined by the ASTM D5708 method. The invention also provides a method for obtaining a crude product, comprising: contacting a crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has, per gram of crude feed: an oxygen content of at least 0.0001 grams of oxygen, and a sulfur content of at least 0.0001 grams of sulfur, and at least one of the catalysts comprises one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof; and controlling contact conditions such that the crude product has an oxygen content of not more than 90% of the oxygen content of the crude feed, and the raw product has a sulfur content of 70-130% of the sulfur content of the crude feed, where the oxygen content is as determined by the ASTM E385 method, and the sulfur content is as determined by the ASTM method D4294. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has per gram of crude feed, a total content of Ni / V / Fe of at least 0.00002 grams, and a sulfur content of at least 0.0001 grams of sulfur, and at least one of the catalysts comprises one or more metals from column 6 of the Periodic Table, or one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof; and controlling contact conditions, such that the crude product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, and the raw product has a sulfur content 70-130% of the sulfur content of the crude feed, where the Ni / V / Fe content is as determined by the ASTM D5708 method, and the sulfur content is as determined by the ASTM D4294 method. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed comprises one or more alkali metal salt of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, the crude feed has per gram of crude feed, a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.00001 grams, and a residual content of at least 0.1 grams of residue, and at least one of the catalysts comprises one or more metals of column 6 of the Periodic Table, one or more compounds of one or more metals of column 6 of the Periodic Table, or mixtures thereof; and control contact conditions such that the crude product has a total content of alkali metal, alkaline earth metal in metal salts of organic acids of not more than 90% or the content of alkali metal, and alkaline earth metal, in metal salts of organic acids in the crude feed, the crude product has a residual content of 70-130% of the residual content of the crude feed, and where the content of alkali metal, alkaline earth metal, in metal salts of organic acids is as determined by the method ASTM D1318, and the residual content is as determined by the method ASTM D5307. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has per gram of crude feed, a total Ni / V / Fe content of at least 0.00002 grams, and at least one of the catalysts comprises one or more metals from column 6 of the Periodic Table, or one or more compounds of one or more metals from column 6 of the Periodic Table, or their mixtures; and controlling contact conditions, such that the crude product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, and the crude product has a residual content of 70-130% of the residual content of the crude feed, where the Ni / V / Fe content is as determined by the ASTM D5708 method, and the residual content is as determined by the ASTM D5307 method. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, the crude feed has per gram of crude oil, a vacuum gas oil ("VGO") of at least 0.1 grams, and a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.0001 grams, and minus one of the catalysts comprises one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or "their mixtures; contact conditions such that the raw product has a total content of alkali metal, and alkaline earth metal in metal salts of organic acids of not more than 90% of the alkali metal content, and an alkaline earth metal, in metal salts of organic acids of the crude feed, and the raw product has a VGO content of 70-130% of the VGO content of the crude feed, where the VGO content is as determined by the ASTM D5307 method, and the alkali metal content, and Alkaline earth metal in metal salts of organic acids is as determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more - catalysts to obtain a total product including the crude product, wherein the crude product is a liquid mixture at 25%. ° C and 0.101 MPa, the crude feed has per gram of crude feed, a total content of Ni / V / Fe of at least 0.00002 grams, and a VGO content of at least 0.1 grams, and at least one of the catalysts comprises one or more metals from column 6 of the Periodic Table, or one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof; and controlling contact conditions, such that the raw product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, and the raw product has a VGO content 70-130% of the VGO content of the crude feed, where the VGO content is as determined by the ASTM D5307 method, and the Ni / V / Fe content is as determined by the ASTM D5708 method. The invention also provides a method for obtaining a crude product, comprising: contacting a crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed includes one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or their mixtures, and the crude feed has, for example, gram of crude feed, a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of at least 0.00001 grams, and at least one of the catalysts is obtained: combining the base with one or more metals of the column 6 of the Periodic Table, one or more compounds of one or more metals from column 6 of the Periodic Table, or their mixtures to produce a catalyst precursor; and forming the catalyst by heating a catalyst precursor in the presence of one or more sulfur-containing compounds at a temperature below 400 ° C; and controlling contact conditions such that the crude product has a total content of alkali metal, and alkaline earth metal, in metal salts of organic acids of not more than 90% of the alkali metal content, and alkaline earth metal, in metal salts of acids organic in the crude feed, wherein the content of alkali metal, and alkaline earth metal in metal salts of organic acids is as determined by the method ASTM D1318. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 °. C and 0.101 MPa, the crude feed has, per gram of the crude feed, a total content of Ni / V / Fe of at least 0.00002 grams and at least one of the catalysts is obtained: by combining a base with one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof, to produce a catalyst precursor; and forming the catalyst by heating the catalyst precursor in the presence of one or more sulfur-containing compounds at a temperature below 400 ° C; and controlling contact conditions such that the product has a total Ni / V / Fe content of not more than 90% of the Ni / V / Fe content of the crude feed, where the Ni / V / Fe content is as it is determined by the method ASTM D5708.

The invention also provides a crude composition having, per gram of crude composition: at least 0.001 grams of hydrocarbons with a boiling point range between 95 ° C and 260 ° C at 0.101 MPa; at least 0.001 grams of hydrocarbons with a boiling range between 260 ° C and 320 ° C at 0.101 MPa; at least 0.001 grams of hydrocarbons with a distribution in the boiling range between 320 ° C and 650 ° C at 0.101 MPa; and greater than 0 grams but less than 0.01 grams of one or more catalysts per gram of the crude product. The invention also provides a crude composition having, per gram of crude composition: at least 0.01 grams of sulfur, as determined by the method ASTM D4294; at least 0.2 grams of residue, as determined by the ASTM D5307 method and the composition has a weight ratio of the MCR content to the C5 asphaltenes content of at least 1.5, where the MCR content is as determined by the method ASTM D5430 and the content of asphaltenes C5 is as determined by the ASTM D2007 method. The invention also provides a method for obtaining a crude product, comprising: contacting the crude feed with one or more catalysts to obtain a total product including the crude product, where the crude product is condensable at 25 ° C and 0.101 MPa, the crude feed has an MCR content of at least 0.00 1 grams per gram of crude feed, and at least one of the catalysts is obtained by: the combination of a base with one or more metals from column 6 of the Periodic Table, one or more compounds of one or more metals from column 6 of the Periodic Table, or mixtures thereof, to produce a catalyst precursor; and forming the catalyst by heating the catalyst precursor in the presence of one or more compounds that it contains. Sulfur at a temperature below 500 ° C; and controlling contact conditions such that the product has an MCR content of not more than 90% of the MCR of the crude feed, where the MCR content is as determined by the ASTM D4530 method. The invention also provides a method for obtaining a crude product, comprising: contacting a crude feed with one or more catalysts to obtain a total product including a crude product, wherein the crude product is condensable at 25 ° C and 0.101 MPa, the crude feed has an MCR content of at least 0.001 grams per gram of crude feed, and at least one of the catalysts has a pore size distribution with an average pore diameter in the range of 70 Á at 180 A, with at least 60% of the total number of pores in the pore size distribution having a pore diameter within 45 A of the average pore diameter, where the pore size distribution is as determined by the ASTM D4282 method; and controlling contact conditions such that the crude product has an MCR of not more than 90% of the MCR of the crude feed, where the MCR is as determined by the ASTM D4530 method. The invention also provides a composition of "crude having, per gram of composition: not more than 0.004 grams of oxygen, as determined by the ASTM E385 method, not more than 0.003 grams of sulfur, as determined by the ASTM method D4294 and at least 0.3 grams of residue, as determined by ASTM method D5307.The invention also provides a crude composition having, per gram of composition: not more than 0.004 grams of oxygen, as determined by the ASTM E385 method No more than 0.003 grams of sulfur, as determined by the ASTM D4294 method, not more than 0.04 grams of basic nitrogen, as determined by the ASTM D2896 method, at least 0.2 grams of residue, as determined by the ASTM method D5307, and the composition has a TAN index of not more than 0.5, as determined by the method ASTM D664. The invention also provides a crude composition having, per gram of composition: at least 0.001 grams of sulfur, as determined by the ASTM method D4294; at least 0.2 grams of residue, as determined by the ASTM D5307 method and the composition has a weight ratio of the MCR content to the C5 asphaltenes content of at least 1.5, and the composition has a TAN index of not more than 0, 5, where the TAN index is as determined by the ASTM D664 method, the MCR weight is as determined by the ASTM method D4530, and the weight of the C5 is as determined by the ASTM D2007 method. In some embodiments, the invention also provides, in combination with one or more of the methods or compositions according to the invention, the crude feed that: (a) has not been treated in a refinery, distilled, and / or fractionally distilled; (b) has components that have a carbon number above 4, and the crude feed has at least 0.5 grams of such components per gram of the crude feed; (c) comprises hydrocarbons, a portion which has: a distribution in the range of boiling point below 100 ° C to 0.101 MPa, a distribution in the range of boiling point between 100 ° C and 200 ° C to 0.101 MPa, a distribution in the boiling range between 200 ° C and 300 ° C at 0.101 MPa, a distribution in the boiling range between 300 ° C and 400 ° C at 0.101 MPa, and a distribution in the boiling range between 400 ° C and 650 ° C at 0.101 MPa; (d) has, per gram of crude feed, at least: 0.001 grams of hydrocarbons having a distribution in the range of boiling point below 100 ° C to 0.101 MPa, 0.001 grams of hydrocarbons having a distribution in 1 boiling point range between 100 ° C and 200 ° C to 0.101 MPa, 0.001 grams of hydrocarbons having a boiling point range between 200 ° C and 300 ° C at 0.101 MPa, 0.001 grams of hydrocarbons they have a distribution in the range of boiling between 300 ° C and 400 ° C to 0.101 MPa, and 0.001 grams of hydrocarbons having a distribution in the boiling range between 400 ° C and 650 ° C at 0.101 MPa; (e) it has a TAN index of at least 0.1, at least 0.3 or in the range of 0.3 to 20, 0.4 to 10, or 0.5 to 5; (f) has an initial boiling point of at least 200 ° C at 0.101 MPa; (g) comprises nickel, vanadium and iron; (h) has at least 0. 00002 grams of Ni / V / total Fe per gram of crude feed; (i) includes sulfur; (j) has at least 0.0001 grams or 0.05 grams of sulfur per gram of crude feed; (k) has at least 0.001 grams of VGO per gram of crude feed; (1) has at least 0.1 grams of residue per gram of crude feed; (m) comprises hydrocarbons containing oxygen; (n) one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or mixtures thereof; (o) comprises at least one zinc salt of an organic acid; and / or (p) comprises at least one arsenic salt of an organic acid.

In some embodiments, the invention also provides, in combination with one or more of the methods or compositions according to the invention, the crude feed that can be obtained by removing naphtha and the more volatile compounds than naphtha from the crude. In some embodiments, the invention also provides, in combination with one or more of the methods or compositions according to the invention, a contact method of a crude feed with one or more catalysts to produce a total product including the crude product in which the curdo feed and the crude product have a content of C5 asphaltenes and an MCR content, and: (a) a sum of the C5 asphaltene content of the crude feed and the MCR content of the crude feed which is S, a sum of the asphaltene content Cs of the crude product and the MCR content of the crude product that is S ', and the contact conditions are controlled in such a way that S' is of maximum 99% of S; and / or (b) the contact conditions are controlled such that the weight ratio of the MCR content of the crude product and the asphaltene content Cs is in the range of 1.2 to 2.0 or 1.3 to 1.9. In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a source of hydrogen, in which the source of hydrogen is: (a) gaseous; (b) hydrogen gas; (e) methane; (d) light hydrocarbons; (e) inert gas; and / or (f) mixtures thereof. In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a contact method of a crude feed with one or more catalysts for producing a total product including the crude product wherein the crude feed is contacted in a contact zone that is in or coupled to an offshore installation In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a method comprising contacting a crude feed with one or more catalysts in the presence of a gas and / or hydrogen source and controlling the contact conditions in such a way that: (a) the ratio of the source of gaseous hydrogen and the crude feed is in the range of 5-800 standard cubic meters of hydrogen gas source per meter c bico feed oil into contact with one or more catalysts; (b) the selected rate of net uptake of hydrogen is controlled by varying the partial pressure of the hydrogen source; (c) the rate of hydrogen uptake is such that the crude product has a TAN index of less than 0.3, but the uptake of hydrogen is less than the amount of hydrogen uptake that would cause substantial phase separation between the feed of crude oil and the total product during the contact; (d) the selected rate of hydrogen uptake is in the range of 1-30 or 1-80 standard cubic meters of the hydrogen source, per cubic meter of crude feed; (e) the gas velocity per hour and / or the source of hydrogen is at least 11 h ~ a, at least 15 h "" 1, or maximum 20 h_1; (f) the partial pressure of the gas and / or hydrogen source during the contact is controlled; (g) the contact temperature is in the range of 50-500 ° C, the speed per hour of total liquid of the gas source and / or hydrogen is in the range of 0.1-30 h "1, and the pressure total gas and / or hydrogen source is in the range of 1.0-20 MPa; (h) the flow of the gas and / or hydrogen source is in the opposite direction to the flow of the crude feed; crude product has an H / C ratio of 70-130% with respect to the H / C index of the crude feed, (j) the uptake of hydrogen by the crude feed is of maximum 80 and / or is in the range of 1-80 or 1-50 normal cubic meters of hydrogen per cubic meter of crude feed, (k) the crude product has a total content of Ni / V / Fe of maximum 90%, 50% or maximum 10% of the Ni content / V / Fe of the crude feed; (1) the raw product has a sulfur content of 70-130% or 80-120% of the sulfur content of the crude feed; (m) the crude product or has a VGO content of 70-130% or 90-110% of the VGO content of the crude feed; (n) the crude product has a residual content of 70-130% or 90-11 0% of the residual content of the crude feed; (o) the crude product has a maximum oxygen content of 90%, 70%, 50%, 40%, or maximum 10% of the oxygen content of the crude feed; (p) the crude product has a total content of alkali metal, alkaline earth metal, in metallic salts of organic acids of maximum 90%, 50%, or maximum 10% of the alkali metal content, and alkaline earth metal, in metal salts of acids organic in the raw food; (q) the P value of the crude feed, during contact, is at least 1.5; (r) the viscosity of the crude product at 37.8 ° C is maximum 90%, 50%, or maximum 10% of the viscosity of the crude feed at 37.8 ° C; (s) the crude product has an API gravity of 70-130% of the API gravity of the crude feed; and / or (t) the crude product has a TAN index of maximum 90%, 50%, 30%, 20%, or maximum 10%, of the TAN index of the crude feed and / or in the range of 0.001 to 0.5 , 0.01 to 0.2, or 0.05 to 0.1. In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a method comprising contacting a crude feed with one or more catalysts and controlling the contact conditions to reduce the content of organic oxygen containing compounds in which: (a) a content of selected organic oxygen compounds is reduced such that the crude product has an oxygen content of maximum 90% of the oxygen content of the crude feed; (b) at least one of the organic oxygen-containing compounds comprises a metal salt of carboxylic acid; (c) at least one compound of the organic oxygen containing compounds comprises an alkali metal salt of carboxylic acid; (d) at least one compound containing organic oxygen comprises an alkaline earth metal salt of a carboxylic acid; (e) at least one compound containing organic oxygen comprises a metal salt of carboxylic acid, wherein the metal comprises one or more metals from column 12 of the Periodic Table; (f) the crude product has a content of organic compounds that do not contain non-carboxylic acids of maximum 90% of the content of organic compounds that do not contain carboxylic in the crude feed; and / or (g) at least one of the oxygen-containing compounds in the crude feed originates from naphthenic acid or organic oxygen compounds that do not contain carboxylic acid. In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a method comprising contacting the crude feed with one or more catalysts wherein: (a) the crude feed it is contacted with at least one of the catalysts at a first temperature, followed by contact at a second temperature, and the contact conditions are controlled in such a way that the first contact temperature is at least 30 ° C lower than the second contact temperature; (b) the crude feed is contacted with hydrogen at a first hydrogen uptake condition, and then at a second hydrogen uptake condition, and the temperature of the first contact condition is at least 30 ° C lower what temperature of the second contact condition; (c) the crude feed is contacted with at least one of the catalysts at a first temperature followed by contact at a second temperature, and the contact conditions are controlled such that the first contact temperature is maximum 200 ° C less than the second contact temperature; (d) hydrogen gas is generated during the contact; (e) hydrogen gas is generated during the contact and the contact conditions are also controlled such that the uptake of the crude feed is at least a portion of the generated hydrogen; (f) the crude feed is contacted with a first and second catalysts, and the contact of the raw feed and the first catalyst forms a crude initial product, and wherein the raw initial product has a TAN index of maximum 90 % of the TAN index of the crude feed; and the contact of the crude initial product with the second catalyst forms a crude product, and where the raw product has a TAN index of maximum 90% of the TAN index of the crude initial product; (g) the contact is made in a stacked bed reactor; (h) the contact is made in a boiling bed reactor; (i) the crude feed is contacted with an additional catalyst subsequent to contact with one or more catalysts; (j) one or more of the catalysts is vanadium and the crude feed is contacted with an additional catalyst in the presence of a hydrogen source subsequent to contact with the vanadium catalyst; (k) hydrogen is generated at a rate that is in the range of 1-20 normal cubic meters, per cubic meter of crude feed; (1) hydrogen is generated during the contact, the crude feed is contacted with an additional catalyst in the presence of a gas and at least a portion of the generated hydrogen, and the contact conditions are controlled in such a way that the flow of gas is in the opposite direction to that of the curdo feed flow and to the generated hydrogen flow; () The crude feed is contacted with a vanadium catalyst at a first temperature and subsequent with an additional catalyst at a second temperature, and the contact conditions are controlled so that the first temperature is at least 30 °. C less than the second temperature; (n) hydrogen gas is generated during the contact, the crude feed is contacted with an additional catalyst, and the contact conditions are controlled such that the additional catalyst captures at least a portion of the generated hydrogen; and / or (o) the crude feed is subsequently contacted with an additional catalyst at a second temperature, and the contact conditions are controlled such that the second temperature is at least 180 ° C. In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a method comprising contacting the crude feed with one or more catalysts wherein: (a) the catalyst is a catalyst with base and the base comprises alumina, silica, silica-alumina, titanium oxide, zirconium oxide, magnesium oxide, or mixtures thereof; (b) the catalyst is a catalyst with base and the base is porous; (c) the method further comprises an additional catalyst that has been heat treated at a temperature above 400 ° C prior to sulfurization; (d) the life of at least one of the catalysts is at least 0.5 years; and / or (e) at least one of the catalysts is in a fixed or suspended bed in the crude feed. In some modalities, the invention also provides, in combination with one or more methods or compositions according to the invention, a method comprising contacting a crude feed with one or more catalysts, at least one of the catalysts is a catalyst with base or a crude metal catalyst and the base catalyst or the crude metal catalyst: (a) comprises one or more metals of columns 5 to 10 of the Periodic Table, one or more compounds of one or more metals of the column 5 to 10 in the Periodic Table, or mixtures thereof; (b) has, per grams of catalyst, at least 0.0001 grams, from 0.0001 to 0.6 grams, or from 0.001 to 0.3 grams of: one or more metals from columns 5 to 10 of the Periodic Table, one or more compounds of one or more metals of columns 5 to 10 of the Periodic Table, or mixtures thereof; (c) comprises one or more metals of columns 6-10 of the Periodic Table, one or more compounds of one or more metals of columns 6 to 10 of the Periodic Table, or mixtures thereof; (d) comprises one or more metals from columns 7 to 10 of the Periodic Table, one or more compounds of one or more metals from column 7 to 10 of the Periodic Table, or mixtures thereof; (e) has per gram of catalyst, of 0.0001-0.6, from 0.001 to 0.3 grams of: one or more metals from columns 7 to 10 of the Periodic Table, one or more compounds of one or more metals from columns 7 to 10 of the Periodic Table, or mixtures thereof; (f > comprises one or more metals of columns 5 to 6 of the Periodic Table, one or more compounds of one or more metals of columns 5 to 6 of the Periodic Table, or mixtures thereof; one or more metals of columns 5 of the Periodic Table, one or more compounds of one or more metals of column 5 of the Periodic Table, or mixtures thereof, (h) has, per gram of catalyst, at least 0.0001 grams, from 0.0001 to 0.6 grams, 0.001 to 0.3 grams, 0.005 to 0.1 grams, or 0.01 to 0.08 grams of: one or more metals from column 5 of the Periodic Table, one or more compounds from one or more metals in the column 5 of the Periodic Table, or mixtures thereof, (i) comprises one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures of the same, (j) has, per gram of catalyst, from 0.0001 to 0.6 grams, 0.001 to 0.3 grams, from 0.005 to 0.1 grams, from 0.01 to 0 .08 grams of one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures of the same; (k) comprises one or more metals from column 10 of the Periodic Table, one more compounds of one or more metals from column 10 of the Periodic Table, or mixtures thereof; (1) has, per gram of catalyst, 0.001 to 0.6 grams or 0.00 1 to 0.3 grams of: one or more metals from column 10 of the Periodic Table, one or more compounds from one or more metals from column 10 of the Periodic Table, or mixtures thereof; (m) comprises vanadium, one or more vanadium compounds, or mixtures thereof; (n) comprises nickel, one or more nickel compounds, or mixtures thereof; (o) comprises cobalt, one or more cobalt compounds, or mixtures thereof; (p) comprises molybdenum, one or more molybdenum compounds, or mixtures thereof; (q) has, per gram of catalyst, from 0.001 to 0.3 or 0.005 to 0.1 grams of: molybdenum, one or more molybdenum compounds, or mixtures thereof; (r) comprises tungsten, one or more tungsten compounds, or mixtures thereof; (s) has, per gram of catalyst, 0.00 to 0.3 grams of: tungsten, one or more tungsten compounds, or mixtures thereof; (t) comprises one or more metals from column 6 of the Periodic Table and one or more metals from column 10 of the Periodic Table, wherein the molar ratio of the metal of column 10 and the metal of column 6 is 1 to 5; (u) comprises one or more elements of column 15 of the Periodic Table, one or more compounds of one or more elements of column 15 of the Periodic Table, or mixtures thereof; (v) has, per gram of catalyst, from 0.00001 to 0.06 grams of: one or more elements of column 15 of the Periodic Table, one or more compounds of one or more elements of column 15 of the Periodic Table, or mixtures thereof; (w) phosphorus, one or more phosphorus compounds, or mixtures thereof; (x) has a maximum 0.1 gram of alpha alumina per gram of catalyst; e / o (y) has at least 0.5 grams of theta alumina per gram of catalyst. In some modalities, the invention also provides, in combination with one or more of the methods or compositions according to the invention, a method for forming a catalyst comprising combining a base with one or more metals to form a base / metal mixture, wherein the base comprises theta alumina, and heat treating the theta alumina / metal base mixture at a temperature of at least 400 ° C, and further comprising: (a) combining the base / metal mixture with water to form a paste, and extrude the pasta; (b) obtaining theta alumina by heat treatment of alumina at a temperature of at least 800 ° C; and / or (e) sulfurizing the catalyst. In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a method comprising the crude feed contact with one or more catalysts, wherein the pore size distribution of the less one of the catalysts has: (a) a mean pore diameter of at least 60 Á, 9-0 Á, 180 Á, 200 A, 230 A, at least 300 Á, maximum 230 Á, maximum 500 A, or in the range of 90-180 Á, 100-140 Á, 120-130 A, 230-250 A, 180-500 Á, 230-500 A, or 60-300 Á; (b) at least 60% of the total number of pores has a pore diameter within 45 A, 35 A, or 25 A, of the average pore diameter; (c) a surface area of at least 60 m2 / g, at least 90 m2 / g, 100 m2 / g, 120 m2 / g, 150 m2 / g, 200 m2 / g, or at least 220 m2 / g; and / or (d) a total volume of all pores of at least 0.3 cm3 / g, 0.4 cm3 / g, 0.5 cm3 / g, or at least 0.7 cm3 / g. In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a method comprising contacting the crude feed with one or more base catalysts, wherein the base: (a) ) comprises alumina, silica, silica-alumina, titanium oxide, zirconium oxide, magnesium oxide, or mixtures thereof, and / or zeolite; (b) comprises alumina and / or delta alumina range; (e) has per gram of base, at least 0.5 grams of alumina range; (d) has, per gram of base, at least 0.3 grams or at least 0. 5 grams of theta alumina; (e) comprises alpha alumina, range alumina, delta alumina, theta alumina, or mixtures thereof; (f) has a maximum 0.1 gram of alpha alumina per gram of base.

In some embodiments, the invention also provides in combination with one or more of the methods or compositions according to the invention, a vanadium catalyst that: (a) has a pore size distribution with an average pore diameter of at least 60 A: (b) comprises a base, which comprises theta alumina, and the vanadium catalyst has a pore size distribution with an average diameter of at least 60A; (c) comprises one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof; and / or (d) has per gram of catalyst, at least 0.001 grams of: one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof. In some embodiments, the invention also provides in combination with one or more of the methods or compositions according to the invention, a crude product has: (a) a TAN index of maximum 0.1, 0.001 to 0.5, 0.01 to 0.2; or from 0.05 to 0.1; (b) maximum 0.000009 grams of alkali metal, and alkaline earth metal, in metal salts of organic acids per gram of crude product; (e) maximum 0.00002 grams of Ni / V / Fe per gram of crude product; and / or (d) more than 0 grams, but less than 0.01 grams, of at least one of the catalysts per gram of crude product.

In some embodiments, the invention also provides, in combination with one or more of the methods or compositions according to the invention, one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more acids organic, or mixtures thereof wherein: (a) at least one of the alkali metals is lithium, sodium, or potassium; and / or (b) at least one of the alkaline earth metals is magnesium or calcium. In some embodiments, the invention also provides, in combination with one or more methods or compositions according to the invention, a method comprising contacting the crude feed with one or more catalysts to produce a total product including a crude product. , the method further comprises: (a) combining the crude product with the crude that is the same or different from the crude feed to form a suitable mixture for transport; (b) combine the crude product with the crude oil that is the same or different from the crude feed to form a suitable mixture for the treatment facilities; (c) fractionating the crude product; and / or (d) fractionating the crude product into one or more distilled fractions, and producing the transport fuel from at least one of the distilled fractions. In some embodiments, the invention also provides in combination with one or more of the methods or compositions according to the invention, a catalyst composition with base that: (a) at least 0.3 grams or at least 0.5 grams of theta alumina per gram of base; (b) comprises delta alumina in the base; (c) has a maximum 0.1 gram of alpha alumina per gram of base; (d) has a pore size distribution with a mean pore diameter of at least 230 A; (e) has a pore pore volume of the pore size distribution of at least 0.3 cm3 / g or at least 0.7 cm3 / g; (f) has a surface area of at least 60 m2 / g or at least 90 m2 / g; (g) comprises one or more metals of columns 7 to 10 of the Periodic Table, one or more compounds of one or more metals of columns 7 to 10 of the Periodic Table, or mixtures thereof; (h) comprises one or more metals from column 5 of the Periodic Table, one or more compounds from one or more metals from column 5 of the Periodic Table, or mixtures thereof; (i) has, per gram of catalyst, from 0.0001 to 0.6 grams or from 0.001 to 0.3 grams of: one or more metals from column 5, one or more metal compounds from column 5, or mixtures thereof; (j) comprises one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof; (k) has, per gram of catalyst, from 0.0001 to 0.6 grams or from 0.001 to 0.3 grams of: one or more metals from column 6, one or more metal compounds from column 6, or mixtures thereof; (1) comprises vanadium, one or more vanadium compounds, or mixtures thereof; (m) comprises molybdenum, one or more molybdenum compounds, or mixtures thereof; (n) comprises tungsten, one or more tungsten compounds, or mixtures thereof, (o) comprises cobalt, one or more cobalt compounds, or mixtures thereof, and / or (p) comprises nickel, one or more nickel compounds or mixtures thereof In some embodiments, the invention also provides in combination with one or more of the methods or compositions according to the invention, a crude composition that: (a) has a TAN index of maximum 1, 0.5, 0.3 or maximum 0.1, (b) has, per gram of composition, at least 0.001 grams of hydrocarbons with a boiling range distribution between 95 ° C and 260 ° C at 0.101 MPa, at least 0.001 grams, at less 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling range distribution between 260 ° C and 320 ° C to 0.101 MPa, and at least 0.001 grams of hydrocarbons with a boiling range distribution between 320 ° C and 650 ° C to 0.101 MPa; (e) has at least 0.0005 grams of nitro basic gene per gram of composition; (d) has, by gram of composition, at least 0. 00 1 grams or at least 0.01 grams of total nitrogen; I (e) has maximum 0.00005 grams of nickel and total vanadium per gram of composition.

In some embodiments, the invention also provides in combination with one or more of the methods or compositions according to the invention, a crude composition that includes one or more catalysts and at least one of the catalysts: (a) has a distribution of pore size with a diameter of by means of at least 180 A, maximum 500 A, and / or in a range of 90 to 180 A, 100 to 140 A, 120 to 130 A; (b) has a mean pore diameter of at least 90 A, with more than 60% of the total number of pores in the pore size distribution having a pore diameter within 45 A, 35 A, or 25 A of the average pore diameter: (c) has a surface area of at least 100 m2 / g, at least 120 m2 / g, or at least 220 m2 / g; (d) comprises a base; and the base comprises alumina, silica, silica-alumina, titanium oxide, zirconium oxide, magnesium oxide, zeolite, and / or mixtures thereof; (e) comprises one or more metals of columns 5 to 10 of the Periodic Table, one or more compounds of one or more metals of columns 5 to 10 of the Periodic Table, or mixtures thereof; (f) comprises one or more metals from column 5 of the Periodic Table, one or more compounds from one or more metals from column 5 of the Periodic Table, or mixtures thereof; (g) has, per gram of catalyst, at least 0.0001 grams of: one or more metals from column 5, one or more metals from column 5, or mixtures thereof; (h) comprises one or more metals from column 6 of the Periodic Table, one or more compounds from one or more metals from column 6 of the Periodic Table, or mixtures thereof; (i) has, per gram of catalyst, at least 0.0001 grams of: one or more metals from column 6, one or more metal compounds from column 6, or mixtures thereof; (j) comprises one or more metals from column 10 of the Periodic Table, one or more compounds from one or more metals from column 10 of the Periodic Table, or mixtures thereof; and / or (k) comprises one or more elements of column 15 of the Periodic Table, one or more compounds of one or more elements of column 15 of the Periodic Table, or mixtures thereof. In other embodiments, the characteristics of the specific embodiments of the invention may be combined with the characteristics of other embodiments of the invention. For example, the characteristics of one embodiment of the invention can be combined with the characteristics of any other modality. In other embodiments, the crude products can be obtained by any of the methods and systems described herein. In other modalities, additional features may be added to specific modalities described herein.

BRIEF DESCRIPTION OF THE FIGURES The advantages of the present invention will be apparent to those skilled in the art with the benefit of the following detailed description and with reference to the appended figures in which: Figure 1 is a schematic of one embodiment of a system of Contact. Figures 2A and 2B are schematics of contact system modalities including two contact zones. Figures 3A and 3B are schematics of contact system modalities that include three contact zones. Figure 4 is schematic of a mode of a separation zone in combination with a contact system. Figure 5 is schematic of one embodiment of a mixing zone in combination with a contact system. Figure 6 is schematic of one embodiment of a combination of a separation zone, a contact system and a mixing zone. Figure 7 is a tabulation of the representative properties of the crude feed and the crude product for a contact mode of the crude feed with three catalysts. Figure 8 is a graphic representation of the bed temperature heavy average versus the length of the execution for a contact mode of the crude feed with one or more catalysts. Figure 9 is a tabulation of representative properties of the crude feed and crude product for a contact mode of the crude feed with two catalysts. Figure 10 is another tabulation of the representative properties of the crude feed and crude product for a contact mode of the crude feed with two catalysts. Figure 11 is the tabulation of the crude feed and the crude products for contact modalities of the crude feed with four different catalyst systems. Figure 12 is a graphical representation of the P value of the crude products versus the execution time for contact modes of the crude feeds with four different catalyst systems. Figure 13 is a graphical representation of net hydrogen uptake by crude feeds versus run time for contact modes of crude feeds with four different catalyst systems. Figure 14 is a graphic representation of the residual content, expressed in percentage by weight, of the crude products versus the execution time for contact modalities of the crude feeds with four different catalyst systems. Figure 15 is a graphical representation of the change in API gravity of the crude products versus the execution time for contact modes of the crude feed with four different catalyst systems. Figure 16 is a graphical representation of the oxygen content, expressed in percent by weight, of crude products versus the execution time for contact modes of crude feeds with four different catalyst systems. Figure 17 is the tabulation of the representative properties of the crude feed and of the crude products for contact modalities of the crude feed with catalyst systems including various amounts of molybdenum catalyst and vanadium catalyst, with a catalyst system which includes a vanadium catalyst and a molybdenum / vanadium catalyst, and with glass beads. Figure 18 is a tabulation of the properties of the crude feed and the crude products for contact modes of the crude feeds with one or more catalysts at various liquid speeds per hour.

Figure 19 is the tabulation of properties of crude feeds and crude products for contact modes of crude feeds at various contact temperatures. While the invention is susceptible to various modifications and alternative forms,. specific embodiments thereof are shown by way of example in the figures. The figures may not be to scale. It should be understood that the figures and the detailed description of the invention are not intended to limit the invention to the particular form described, but on the contrary, it is intended to cover all modifications, equivalences and alternatives which are within the spirit and scope of the present invention as defined in the appended claims.

DETAILED DESCRIPTION OF THE INVENTION In the present description certain embodiments of the inventions are described in more detail. The terms used herein are defined as follows. "ASTM" is the American Standard Testing and Materials. "Gravity API" is API gravity at 15.5 ° C (60 ° F). The API gravity is the one determined by the ASTM method D6822. The percentage of atomic hydrogen and the percentage of atomic carbon of the crude feed and crude product are those determined by the ASTM D5291 method. The boiling range distributions of the crude feed, the total product or the raw product are those determined by the ASTM D5307 method unless otherwise indicated. The "C5 asphaltenes" are insoluble asphaltenes in pentane. The content of asphaltenes C5 is that determined with the ASTM D2007 method. The metals in Column X "refer to one or more metals from Column X of the Periodic Table or to one or more compounds from one or more metals from Column X of the Periodic Table, where X is the number of Column (for example, 1 to 12) of the Periodic Table For example, "the metals of Column 6" describe one or more metals from Column 6 of the Periodic Table or one or more compounds from one or more metals of Column 6 of the Periodic Table. "Elements of Column X" refer to one or more elements of Column X of the Periodic Table or to one or more compounds of one or more elements of Column X of the Periodic Table, in which X is the Column number (for example 13 to 18) of the Periodic Table For example, "the elements of Column 15" describe one or more elements of Column 15 of the Periodic Table or one or more compounds of one or more elements of Column 15 of the Periodic Table. application, the weight of a metal of the Periodic Table, the weight of a compound of a metal of the Periodic Table, the weight of an element of the Periodic Table, or the weight of a compound of an element of the Periodic Table, calculated as the weight of the metal or the weight of the element. For example, if 0.1 grams of Mo03 are used per gram of catalyst, the calculated weight of molybdenum metal in the catalyst is 0.067 grams per gram of catalyst. "Content" means the weight of a component in a substrate (for example, a crude feed, a total product, or a crude product) expressed as a weight fraction or weight percentage based on the total weight of the product. substratum. "Wtpp" are parts per million by weight. "Crude feed mix and total product" is the mixture that comes into contact with the catalyst during processing. "Distillates" are hydrocarbons with boiling range distribution between 204 ° C (400 ° F) and 343 ° C (650 ° F) at 0.101 MPa. Distillate content is that determined by the ASTM D5307 method. "Heteroatoms" are oxygen, nitrogen or sulfur in the molecular structure of a hydrocarbon. The content of heteroatoms is determined by the methods ASTM E385 for oxygen, D5762 for total nitrogen and D4294 for sulfur. "Total basic nitrogen" are the nitrogen compounds that have a pKa of less than 40. The basic nitrogen ("bn") is as determined by the method ASTM.D2896. "Hydrogen source" is hydrogen, or a compound, or compounds that when in the presence of a crude feed and the catalyst react to provide hydrogen to the crude feed compounds. A source of hydrogen may include, but is not limited to, hydrocarbons (for example hydrocarbons from Ci to C4 such as methane, ethane, propane and butane), water, or mixtures thereof. A mass balance can be made to evaluate the net amount of hydrogen added to the crude feed compounds. "Flat plate fractionation force" is the comprehensive force needed to fractionate the catalyst. This flat plate fractioning force is determined by the method ASTM D4179. "LHSV" is the volumetric liquid feed rate per total volume of catalyst, and is expressed in hours (h_1). The total catalyst volume is calculated as the sum of the catalyst volumes in the contact zones, as described herein. "The liquid mixture" is a composition that includes one or more compounds that are liquid at standard temperatures and pressures (25 ° C, 0.101 MPa, indices referred to herein as "STP"), or a composition that includes the combination of one or more compounds that are liquid to STP with one or more compounds that are solid to STP. The "Periodic Table" describes the Periodic Table described by the International Union of Pure and Applied Chemistry (IUPAC), November 2003. "Metals in metallic salts of organic acids" are alkali metals, alkaline earth metals, zinc, arsenic, chromium, or combinations thereof. The content of metals in metal salts of organic acids is determined by the method ASTM D1318. The content of micro-carbon waste ("MCR") means the amount of carbon waste left after evaporation and pyrolysis of the substrate. The MCR content is the one determined by the ASTM D4530 method. '"Naphtha" are the hydrocarbon components with a boiling range distribution between 38 ° C (100 ° F) and 200 ° C (392 ° F) at 0.101 MPa. The content of naphtha is the one determined by the method ASTM D5307. "Ni / V / Fe" is nickel, vanadium, iron or combinations thereof.

"Ni / V / Fe content" is nickel, vanadium, iron or combinations thereof. The content of Ni / V / Fe is that determined by the method ASTM D5708. "Nm3 / m3" are normal cubic meters per cubic meter of gas from the crude feed. "Non-carboxylic compounds containing organic oxygen" are the organic oxygen compounds that do not have the carboxylic group (~ C02-). Non-carboxylic organic oxygen compounds include, but are not limited to, ethers, cyclic ethers, alcohols, aromatic alcohols, ketones, aldehydes, or combinations thereof, which do not have a carboxylic group. "Non-condensable gas" are either components or mixtures of components that are gases to STP. "P value (peptization)" or "P value" is the numerical value, which represents the tendency to flocculate the asphaltenes in the crude feed. The determination of the P value is described in J. J. Heithaus in "Measurement and Significance of Asphaltene Peptization", Journal of Institute of Petroleum, Vol. 48, Number 458, February 1962, pp. 45-53. "Pore diameter", "average pore diameter" and "pore volume" describe the pore diameter, average pore diameter, and pore volume, as determined by the ASTM method D4284 (mercury porosimetry at an angle of 140 ° contact). A micromeritics® A9220 instrument (Micromeritics Inc., Norcross, Georgia, USA) can be used to determine these values. "Residue" means components whose boiling range is above 538 ° C (1000 ° F), as determined by the method ASTM D5307. "SCFB" is the standard cubic foot of gas per barrel of crude feed. "Surface area" of a catalyst is that determined by the ASTM D3663 method. "TAN" is the total acid number expressed as milligrams ("mg") of KOH per gram ("g") of sample. TAN is the index determined by the ASTM D664 method. "VGO" are hydrocarbons with a boiling range distribution between 343 ° C (650 ° F) and 538 ° C (1000 ° F) at 0.101 MPa. The VGO content is the one determined by the ASTM D5307 method. "Viscosity" is the kinematic viscosity at 37.8 ° C (100 ° F). The viscosity is that which is determined using the method ASTM D445. In the context of this application, it is to be understood that if the value obtained for a property of the tested substrate is outside the limits of the test method, it may be modified or recalibrated to study such property.

The crudes can be produced or distilled from the hydrocarbon formations and then stabilized. Crudes may include oil. Generally, the crudes are in solid, semi-solid or liquid state. Stabilization may include, but is not limited to, the removal of non-condensable gases, water, salts or combinations thereof from the crude to form a stabilized crude. This stabilization can usually take place at or near the production or distillation site. Stabilized crudes generally have not been distilled, in whole or in fractions, in the treatment facilities, to produce multiple components with specific boiling point distributions (eg, naphtha, distillates, VGO, or lubricating oils) . Distillation includes, but is not limited to, atmospheric distillation methods or vacuum distillation methods. Unblemished or unfractionated stabilized crudes include components that have a carbon number greater than 4 in amounts of at least 0.5 grams of the components per gram of crude. Examples of stabilized crudes include whole crudes, crudes without head fraction, heartless crudes, crudes without heartless head fraction, or combinations thereof. "Crude without head fraction" is a crude that has been treated in such a way that at least some of the components with boiling points below 35 ° C at 0.101 MPa (95 ° F at 1 atm) have been removed. As usual, crude oils without a head fraction have a maximum content of 0.1 g, maximum 0.05 grams, or maximum 0.02 grams of these components per gram of crude oil without a head fraction. Some stabilized crudes have properties such that stabilized crudes are transported to conventional treatment facilities by transport vehicles (eg pipes, trucks or ships). Other crudes have one or more unsuitable properties that make them disadvantageous. The disadvantageous crudes may not be acceptable for the transport vehicle or for the treatment facilities, which makes the disadvantageous crude have low economic value. The economic value can be such that the production, transport or treatment of the reserve that includes the disadvantageous crude is considered very expensive. The properties of unfavorable crudes include, but are not limited to: a) a TAN index of at least 0.1, at least 0.3; b) viscosity of at least 10 cSt; c) API gravity of maximum 19; d) a total Ni / V / Fe content of at least 0.00002 grams or at least 0.0001 grams of Ni / V / Fe per gram of crude; e) a total heteroatom content of at least 0.005 grams of heteroatoms per gram of crude; f) a waste content of at least 0.01 grams of waste per gram of crude oil; g) a C5 asphaltene content of at least 0.04 grams of C5 asphaltenes per gram of crude; h) an MCR content of at least 0.002 grams of MCR per gram of crude; i) a content of metals in metal salts of organic acids of at least 0.00001 grams of metals per gram of crude; or j) combinations thereof. In some modalities, disadvantageous crude oil may include, per gram of crude bear disadvantage, at least 0.2 grams of residue, at least 0.3 grams of residue, at least 0.5 grams of residue, or at least 0.9 grams of residue. In some modalities, the disadvantageous crude may have a TAN index in the range of 0.1 or 0.3 to 20, 0.3 or 0.5 to 10, or 0.4 or 0.5 to 5. In certain modalities, disadvantageous crude oils, per gram of disadvantageous crude oil, they may have a sulfur content of at least 0.005 grams, at least 0.01 grams, or at least 0.02 grams. In some embodiments, disadvantageous crudes have properties that include, but are not limited to: a) a TAN index of at least 0.5; b) an oxygen content of at least 0.005 grams of oxygen per gram of crude feed; c) a C5 asphaltene content of at least 0.04 grams of C5 asphaltenes per gram of crude feed; d) a higher viscosity than desired (eg,> 10 cSt for a crude feed with an API gravity of at least 10; e) a metal content in metal salts of organic acids of at least 0.00001 grams of metals per gram of crude; or f) combinations thereof. Unfavorable crudes may include per gram of disadvantageous crude: at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with boiling points in the range of 95 ° C and 200 ° C to 0.101 MPa; at least 0.01 grams, at least 0.005 grams, or at least 0.001 grams of hydrocarbons with a boiling point distribution in the range of 200 ° C and 300 ° C to 0.101 MPa; at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling point distribution in the range of 300 ° C and 400 ° C to 0.101 MPa; and at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling point distribution in the range of 400 ° C and 650 ° C to 0.101 MPa. The unfavorable crudes may include, per gram of disadvantageous crude: at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams hydrocarbons with a distribution of boiling points in the range of maximum 100 ° C to 0.101 MPa; at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with distribution of boiling points in the range of 100 ° C and 200 ° C to 0.101 MPa; at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with distribution of boiling points in the range of 200 ° C and 300 ° C to 0.101 MPa; and at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling point distribution in the range of 300 ° C and 400 ° C to 0.101 MPa, and at least 0.001 grams, at least 0.005 grams , or at least 0.01 grams of hydrocarbons with a boiling point distribution in the range of 400 ° C and 650 ° C to 0.101 MPa. Some disadvantageous crudes may include, per gram of disadvantageous crude, at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling point distribution in the range of maximum 100 ° C to 0.101 MPa, in addition to other components with higher boiling ranges. In general, unfavorable crude oil has, per gram of unfavorable crude, a content of such hydrocarbons of maximum 0.2 grams or maximum 0.1 grams. Some disadvantageous crudes may include, per gram of disadvantageous crude, at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with boiling point distribution in the range of maximum 200 ° C to 0.101 MPa. Some disadvantageous crudes may include, per gram of disadvantageous crude, at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons with a boiling point distribution in the range of at least 650 ° C. Among the disadvantageous crudes that can be treated with the processes described herein include, but are not limited to, the crudes obtained from the following regions: Cost of the US Gulf and Southern California, tar sands of Canada, Santos and Campos basin in Brazil, Gulf of Suez in Egypt, Chad, North Sea of the United Kingdom, Offshore in Angola, Bohai Bay China, Zulia in Venezuela, Malaysia, and Sumatra in Indonesia. The treatment of disadvantageous crudes can improve the properties of disadvantageous crudes so that they become acceptable for transportation or for treatment. The crude or a disadvantageous crude that is treated herein is described as "crude feed". The crude feed can be without head fraction, as described herein. The raw product obtained from the crude feed treatment, as described herein, is generally suitable to be transported or to be treated. The properties of the crude product produced as described herein are more similar to the corresponding properties of the West Texas Intermediate crude than to the crude feed, or more similar to the corresponding properties of the Brent crude, than to the feed of crude oil, which improves the economic value of crude oil. This crude product can be refined with less pretreatment or without it, which improves refining efficiency. The pretreatment may include desulfurization, demetallization or atmospheric distillation to remove impurities. The treatment of the crude feed according to the inventions described herein may include the contact of the crude feed with the catalysts in a contact zone or the combinations of two or more contact zones. In a contact zone, at least one property of the crude feed can be changed by the contact of the crude feed with one or more catalysts related to the same property of the crude feed. In some embodiments, the contact is made in the presence of a hydrogen source. In some embodiments, the source of hydrogen is one or more hydrocarbons that under certain contact conditions react to provide relatively small concentrations of hydrogen with respect to the crude feed compounds. Figure 1 is a diagram of the contact system 100 that includes a contact zone 102 A. The crude feed enters the contact zone 102 through the conduit 104. The contact zone can be a reactor, a reactor portion, multiple portions of the reactor, or combinations thereof. Examples of contact zones include a stacked bed reactor, a fixed bed reactor, a boiling bed reactor, a continuous stirred tank reactor ("CSTR"), a fluid bed reactor, a vaporization reactor, and a liquid / liquid switch. In certain modalities, the contact system is located in the offshore installation or is coupled to it. The contact of the crude feed with the catalyst in the contact system 100 can be a continuous process or a batch process. The contact zone may include one or more catalysts (for example, two catalysts). In some embodiments, the contact of the crude feed with a first catalyst of the two catalysts can reduce the TAN index of the crude feed. The subsequent contact of the reduced TAN crude feed with the second catalyst decreases the heteroatom content and increases the API gravity. In other modalities, the TAN index, viscosity, Ni / V / Fe content, heteroatom content, residue content, API gravity, or these combined properties of the crude product change by at least 10% in relation to the same properties of the crude feed then of the contact of the crude feed with one or more catalysts. In certain embodiments, a volume of catalyst in the contact zone is in the range of 10-60% vol, 20-50% vol or 30-40% vol of the total volume of the crude feed in the contact zone . In some embodiments, a catalyst suspension and crude feed may include from 0.001 to 10 grams, from 0.005 to 5 grams, or from 0.01 to 3 grams of catalyst per 100 grams of crude feed in the contact zone. The contact conditions in the contact zone may include, but are not limited to, the temperature, pressure, flow of the hydrogen source, flow of the crude feed, their combinations. The contact conditions in some modalities are controlled in such a way that they produce a crude product with specific properties. The temperature in the contact zone can be 50 to 500 ° C, 60 to 440 ° C, 70 to 430 ° C, or 80 to 420 ° C. The pressure in the contact zone can be 0.1-20 MPa, 1-12 MPa, 4-10 MPa, or 6-8 MPa. Generally, the LHSV of the crude feed is in the range of 0.1-30 hf1, 0.5-25 h_1, 1-20 h "1, 1.5-15 h-1, or 2-10 h" 1. In some modalities, LHSV is at least 5 h_1, at least 11 h-1, at least 15 hf1, or at least 20 h-1.

In embodiments in which the hydrogen source is supplied in the form of a gas (for example, hydrogen gas), the ratio between the source of gaseous hydrogen and the crude feed is in the range of 0.1-100,000 Nm / m 3 , 0.5-10,000 Nm3 / m3, 1-8,000 Nm3 / m3, 2-5,000 Nm3 / m3, 5-3,000 Nm3 / m3, or 10-800 Nm3 / m3 contacted with the catalyst. In some embodiments, the hydrogen source is combined with a carrier gas, which recirculates through the contact zone. The carrier gas can be, for example, nitrogen, helium or argon. The carrier gas can facilitate the circulation of the crude feed and / or the circulation of the hydrogen source in the contact zones. The carrier gas can also improve the mixing in the contact zones. In some embodiments, the source of hydrogen (eg, hydrogen, methane or ethane) can be used as the carrier gas and recirculated through the contact zone. The hydrogen source can enter the contact zone 102 in the same direction of circulation as the crude feed in the conduit 104 or separately through the conduit 106. In the contact zone 102, the contact of the feed of Crude oil with the catalyst allows to obtain a total product that includes a crude product, and in some modalities, a gas. In some embodiments, the carrier gas is combined with the crude feed or with the hydrogen source in the conduit 106. The total product can leave the contact zone 102 and enter the separation zone 108 through the conduit 110. In the separation zone 108, the crude product and the gas can be separated from the total product with generally known separation techniques, for example, separation of gas and liquid. The crude product can leave the separation zone 108 through the conduit 112, and then be transported to the carrier vehicles, pipes, storage vessels, refineries, other processing zones, or combinations thereof. The gas may include gas formed during processing (eg, hydrogen sulfide, carbon dioxide, or carbon monoxide), the source of excess hydrogen gas, or the carrier gas. The excess gas can be recycled to the contact system 100, purified, transported to other processing areas, storage containers, or combinations thereof. In some embodiments, the contact of the crude feed with the catalyst to obtain the total product is carried out in two or more contact zones. The total product can be separated to form the crude product and gases. Figures 2-3 are diagrams of the modalities of the contact system 100 that includes two or three contact zones. In Figures 2A and 2B, the contact system 100 includes the contact zones 102 and 114. Figures 3A and 3B include the contact zones 102, 114 and 116. In Figures 2A and 3A, the contact areas 102, 114 and 116 are detailed as separate contact zones in a reactor. The crude feed enters the contact zone 102 through the conduit 104. In some embodiments, the carrier gas is combined with the hydrogen source in the conduit 106 and is introduced into the contact zones in the form of a mixture. In certain embodiments, as shown in Figures 1, 3A and 3B, the hydrogen source or the carrier gas may enter the contact zone (s) with the crude feed separately through line 106 or well in the opposite direction to the flow of the crude feed, for example, through the conduit 106 '. The addition of hydrogen source or carrier gas contrary to the crude feed flow can maximize the mixing or contact of the crude feed with the catalyst. The contact of the crude feed with catalyst (s) in the contact zone 102 gives rise to the feed stream. The supply current flows from the contact zone 102 to the contact zone 114. In FIGS. 3A and 3B, the feed stream flows from the contact zone 114 to the contact area 116. The contact zones 102, 114 and 116 may include one or more catalysts. As shown in Fig. 2B, the feed stream leaves the contact zone 102 through the conduit 118 and enters the contact area 114. As shown in Fig. 3B, the feed stream leaves the contact area 114 through conduit 118 and enters contact zone 116. The feed stream can be contacted with additional catalysts in contact zone 114 or in contact zone 116 to form the total product. The total product leaves contact zone 114 or contact zone 116 and enters separation zone 108 through line 110. The raw product or gas is separated from the total product. The crude product leaves the separation zone 108 through the conduit 112. Figure 4 is a diagram of an embodiment of a separation zone upstream of the contact system 100. The crude disadvantageous (either crude without fraction of head or not ) enters the separation zone 120 through the conduit 122 .. In the separation zone 120, at least a portion of the disadvantageous crude oil is separated by known techniques in the field (eg, spraying, membrane separation, pressure reduction) to produce the crude feed. For example, water can be at least partially separated from the disadvantageous crude. In another example, the components having boiling ranges below 95 ° C or below 100 ° C can be at least partially separated from the unfavorable crude to produce the crude feed. In some embodiments, at least a portion of the naphtha and more volatile compounds than the naphtha are separated from the disadvantageous crude. In some embodiments, at least a portion of the separated components leaves the separation zone 120 through the conduit 124. The crude feed obtained from the separation zone 120, in some embodiments, includes a mixture of components with an interval distribution. of boiling at least 100 ° C, or in certain embodiments, a boiling range distribution of at least 120 ° C. In general, the separated crude feed includes a mixture of components with a boiling point range distribution of between 100 and 1000 ° C, 120 and 900 ° C, or 200 to 800 ° C. At least a portion of the crude feed leaves the separation zone 120 and enters the contact system 100 (see, for example, the contact zones of Figures 1-3) through the conduit 126 to be processed again and form the raw product. In certain embodiments, the separation zone 120 may be upstream or downstream of the desalination unit. After processing, the crude product leaves the contact system 100 through conduit 112. In certain embodiments, the crude product is mixed with the crude that is the same or different from the crude feed. For example, the crude product can be combined with the crude having different viscosity which results in a product mixed with a viscosity that is between the viscosity of the crude product and the viscosity of the crude oil. In another example, the crude product can be mixed with the crude oil that has a TAN index that is different, which results in a product with a TAN index that is between the TAN index of the crude product and the crude oil. The mixed product may be suitable for transportation and / or treatment. As shown in Figure 5, in certain embodiments, the crude feed enters the contact system 100 through the conduit 104, and at least a portion of the raw product leaves the contact system 100 through the conduit 128 and is introduced in the mixing zone 130. In the mixing zone 130, at least a portion of the raw product is combined with one or more process streams (e.g.a stream of hydrocarbons such as naphtha produced from the separation of one or more feeds of crude), a crude, a crude feed, or mixtures thereof, to produce a mixed product. The process streams, the crude oil feed, or their mixtures are introduced directly into the mixing zone 130 or upstream of such zone through the conduit 132. The mixing system can be located in the mixing zone 130 or nearby to such area. The mixed product can be in accordance with the product specifications designated by the refineries or by transport vehicles. Product specifications include, but are not limited to, an API gravity range or limit, TAN index, viscosity, or combinations thereof. The mixed product leaves the mixing zone 130 through the conduit 134 to be transported or processed. In Figure 6, the disadvantageous crude enters the separation zone 120 through the conduit 122, and the disadvantageous crude is separated as described above to form the crude feed. The crude feed then enters the contact system 100 through the conduit 126. At least some of the components of the disadvantageous crude oil leave the separation zone 120 through the conduit 124. At least a portion of the crude product leaves the zone of separation. 100 contact and enter the mixing zone 130 through the conduit 128. Other streams and / or crude of the process enter the mixing zone 130 directly or through the conduit 132 and combine with the crude product to form a mixed product. The crude product leaves the mixing zone 130 through line 134.

In some modalities, the raw product and / or mixed product is transported to the refinery and / or treatment facility. The raw product or mixed product can be processed to produce commercial products such as transport fuel, heating fuel, lubricants, or chemicals. The processing may include the distillation or fractional distillation of the crude product or blended product to obtain one or more distillation fractions. In some embodiments, the crude product, mixed product or one or more distilled fractions may be hydrotreated. In some modalities, the crude product has a TAN index of maximum 90%, maximum 50%, maximum 30% or maximum 10% of the TAN index of the crude feed. In some embodiments, the crude product has a TAN index in the range of 1 to 80%, 20 to 70%, 30 to 60%, or 40 to 50% of the TAN index of the crude feed. In certain modalities, the raw product has a TAN index of maximum 1, maximum 0.5, maximum 0.3, maximum 0.2, and maximum 0.1 or maximum 0.05. The TAN index of the crude product is commonly at least 0.0001 and, more frequently, at least 0.001. In some embodiments, the TAN index of the crude product can be in the range of 0.001 to 0.5, 0.01 to 0.2 or 0.05 to 0.1. In some modalities, the crude product has a total content of Ni / V / Fe maximum of 90%, maximum 50%, maximum 10% or maximum 5% or maximum 3% of the content of Ni / V / Fe of the crude feed . In some embodiments, the crude product has a total Ni / V / Fe content in the range of 1-80%, 10-70%, 20-60%, or 30-50% of the Ni / V / Fe content of the crude feed. In certain embodiments, the raw product has, per gram of crude product, a total Ni / V / Fe content in the range of 1 x 10"7 grams to 5 x 10" 5 grams, 3 x 10 ~ 7 grams to 2 x 10-5 grams, or 1 x 10-6 grams at 1 x 10-5 grams. In certain modalities, the crude oil has maximum 2 x 10"5 grams of Ni / V / Fe. In some embodiments, the content of Ni / V / Fe total of the raw product is 70-130%, 80-120%, or 90 -110% of the Ni / V / Fe content of the crude feed In some embodiments, the raw product has a total metal content of metallic salts of organic acids of maximum 90%, maximum 50%, maximum 10%, or maximum 5% of the total content of metals in metal salts of organic acids in the crude feed In certain embodiments, the crude product has a metal content in metallic salts of organic acids in a range of 1-80%, 10- 70%, 20-60%, or 30-50% of the total content of the metals in metal salts of organic acids in the crude feed The organic acids that generally form the metal salts, include, but are not limited to, carboxylic acids , thiols, imides, sulphonic acids and sulfonates. boxylic acids include, but are not limited to, naphthenic acids, phenanthrenic acids, and benzoic acid. "The metal portion of metal salts may include alkali metals (eg, lithium, sodium and potassium), alkaline earth metals (eg, magnesium, calcium, and barium), metals from Column 12 (eg, zinc and cadmium). ), metals from Column 15 (for example, arsenic), metals from Column 6 (for example, chromium) or their mixtures thereof In certain embodiments, the crude product has a total content of metals in metallic acid salts organic, per gram of crude product, in the range of 0.0000001 grams to 0.00005 grams, from 0.0000003 grams to 0.00002 grams, or from 0.000001 grams to 0.00001 grams of metals in metal salts of organic acids per gram of crude product. The crude product has a total content of metals in metallic salts of organic acids is 70-130%, 80-120%, 90-110%, of the total content of the metals in metal salts of organic acids in the crude feed. In certain m odalities, the API gravity of the crude product produced by the contact of the crude feed with the catalyst, at contact conditions, it is 70-130%, 80-120%, 90-110% or 100-130% of the API gravity of the crude feed. In certain modalities, the API gravity of the crude product is from 14 to 40, 15 to 30 or 16 to 25. In certain embodiments, the crude product has a viscosity of maximum 90%, maximum 80%, or maximum 70% of the viscosity , of the crude feed. In some embodiments, the crude product has a viscosity in the range of 10-60%, 20-50%, or 30-40% of the viscosity of the crude feed. In some embodiments, the viscosity of the crude product is maximum 90% of the viscosity of the crude feed while the API gravity of the crude product is 70-130%, 80-120%, 090-110% of API gravity of the crude feed. In some embodiments, the crude product has a total heteroatom content of maximum 90%, maximum 50%, maximum 10% or maximum 5% of the total heteroatom content of the crude feed. In certain embodiments, the crude product has a total heteroatom content of at least 1%, at least 30%, at least 80% or at least 99% of the total heteroatom content of the crude feed. In some embodiments, the crude product has a sulfur content that can be a maximum of 90%, 50%, 10% or 5% of the total sulfur content of the crude product. In certain embodiments, the crude product has a sulfur content of at least 1%, at least 30%, at least 80% or at least 99% of the sulfur content of the crude feed. In some embodiments, the sulfur content of the crude product is 70-130%, 80-120%, or 90-110% of the sulfur content of the crude feed. In some embodiments, the crude product has a total nitrogen content that can be maximum 90%, maximum 80%, maximum 10% or maximum 5% of the total nitrogen content of the crude feed. In certain embodiments, the crude product has a total nitrogen content of at least 1%, at least 30%, at least 80% or at least 99% of the total nitrogen content of the crude feed. - In some modalities, the crude product has a basic nitrogen content that can be maximum 95%, maximum 90%, maximum 50% or maximum 10%, or maximum 5% of the basic nitrogen content of the crude feed. In certain embodiments, the crude product has a basic nitrogen content of at least 1%, at least 30%, at least 80% or at least 99% of the basic nitrogen content of the crude feed. In some embodiments, the crude product has an oxygen content that can be a maximum of 90%, 50%, 30%, 10%, or 5% of the oxygen content of the crude feed. In certain embodiments, the crude product has an oxygen content of at least: 1%, 30%, 80% or at least 99% of the oxygen content of the crude feed. In some embodiments, the oxygen content of the crude product is in the range of 1-80%, 10-70%, 20-60%, or 30-50% of the oxygen content of the crude feed. In some embodiments, the total content of carboxylic acid compounds of the crude product may be maximum 90%, 50%, 10%, maximum 5% of the content of carboxylic acid compounds in the crude feed. In some embodiments, the crude product has a total content of carboxylic acid compounds of at least 1%, 30%, 80% or at least 99% of the total content of carboxylic acid compounds of the crude feed. In certain embodiments, the selected organic oxygen compounds can be reduced in the crude feed. In some embodiments, carboxylic acids or metal salts of carboxylic acids can be chemically reduced before organic oxygen compounds that do not contain carboxylic acids. In a crude product, carboxylic acids can be differentiated from non-carboxylic organic oxygen compounds by analyzing the crude product using generally known spectroscopic methods (e.g., infrared analysis, mass spectrometry, or gas chromatography). In some embodiments, the crude product has an oxygen content of maximum 90%, 80%, 70%, or maximum 50% of the oxygen content of the crude feed, and the TAN index of the crude product is of maximum 90%, 70 %, 50%, or maximum 40% of the TAN index of the crude feed. In certain embodiments, the crude product has an oxygen content of at least 1%, 80%, 30%, or at least 99% of the oxygen content of the crude feed, and the TAN index of the crude product is at least 1% , 30%, 80%, or at least 99% of the TAN index of the crude feed. In addition, the crude product may have a content of carboxylic acids or metal salts of carboxylic acids of maximum 90%, 70%, 50%, or maximum 40% of the crude feed, and a content of organic oxygen compounds that do not contain carboxyl of 70-130%, 80-120%, or 90-110% of the organic oxygen compounds that do not contain carboxylic from the crude feed. In certain modalities, the crude product includes, in its molecular structures, from 0.05 to 0.15 grams or from 0.09 to 0.13 grams of hydrogen per gram of raw product. The crude product can include, in its molecular structures, from 0.8 to 0.9 grams or from 0.82 to 0.88 grams of carbon per gram of raw product. The atomic hydrogen to atomic carbon (H / C) rate of the crude product can be 70-130%, 80-120%, or 90-110% of the atomic H / C rate of the crude feed. An atomic H / C rate of the crude product is 10-30% of the atomic H / C rate of the crude feed indicates that the uptake or, the hydrogen consumption in the process is relatively low, and / or that Hydrogen is produced in situ. The crude product includes components with a range of boiling points. In some embodiments, the crude product includes, per gram of crude product: at least 0.001 grams, or from 0.001 to 0.5 grams of hydrocarbons with a boiling range of maximum 100 ° C to 0.101 MPa; at least 0.001 grams, or from 0.001-0.5 grams of hydrocarbons with a distribution in the boiling range between 100 ° C and 200 ° C at 0.101 MPa; at least 0.001 grams, - or from 0.001-0.5 grams of hydrocarbons with a distribution in the boiling range between 200 ° C and 300 ° C at 0.101 MPa; at least 0.00 1 grams, or from 0.001-0.5 grams of hydrocarbons with a distribution in the boiling range between 300 ° C and 400 ° C at 0.101 MPa; at least 0.001 grams, or from 0.001 to 0.5 grams of hydrocarbons with a distribution in the boiling range between 400 ° C and 538 ° C to 0.101 MPa. In some embodiments, the crude product includes, per gram of crude product, at least 0.001 grams of hydrocarbons with a distribution in the boiling range of maximum 100 ° C to 0.101 MPa or at least 0.001 grams of hydrocarbons with distribution in the boiling range between 100 ° C and 200 ° C at 0.101 MPa.

In certain embodiments, the crude product may have at least 0.001 grams, or at least 0.01 grams of naphtha per gram of crude product. In other modalities, the crude product may have a naphtha content of maximum 0.6 grams, or maximum 0.8 grams of naphtha per gram of crude product. In certain embodiments, the distillate content of the crude-product is 70-130%, 80-120%, or 90-110% of the distillate content of the crude feed. The distillate content of the crude product can be found, per gram of crude product, in the range of 0.00001-0.5 grams, 0.001-0.3 grams, or 0.002-0.2 grams. In certain embodiments, the VGO content of the crude product is 70-130%, 80-120%, or 90-110% of the VGO content of the crude feed. In certain modalities, the raw product has, per gram of crude product, a VGO content in the range of 0.00001-0.8 grams, 0.001-0.5 grams, 0.002-0.4 grams, or 0.001-0.3 grams. In some embodiments, the residue content of the crude product is 70-130%, 80-120%, or 90-110% of the residue content of the crude feed. The crude product may have, per gram of crude product, a residue content in the range from 0.00001-0.8 grams, 0.0001-0.5 grams, 0.0005-0.4 grams, 0.001-0.3 grams, .0.005-0.2 grams, or 0.01-0.1. grams. In certain embodiments, the crude product has an MCR content of 70-130%, 80-120%, or 90-110% of the MCR content of the crude feed, while the raw product has a C5 asphaltene content of maximum 90%, 80%, or maximum 50% of the C5 asphaltene content of the crude feed. In certain embodiments, the C5-asphaltene content of the crude feed is at least 10%, 60%, or at least 70% of the C5 asphaltene content of the crude feed while the MCR content of the crude product is 10-30% of the MCR content of the crude feed. In some embodiments, the decrease in the C5 asphaltene content of the crude feed while the MCR content remains relatively stable may increase the stability of the crude feed mix / total product. In certain embodiments, the C5 asphaltene content and the MCR content can be combined to produce a mathematical relationship between the high viscosity components in the crude product relative to the high viscosity components in the crude feed. For example, a sum of the C5 asphaltene content of the crude feed and the MCR content of the crude feed can be represented by S. The sum of the C5 asphaltene content of the crude feed and the MCR content of the crude product it can be represented by S '. The sums can be compared (S'a S) to evaluate the net reduction in high viscosity components in the crude feed. S 'of the crude product may be in the range of 1-99%, 10-90%, or 20-80% of S. In some embodiments, a MCR content rate of the crude product for the C5 asphaltene content is in the range of 1.0-3.0, 1.2-2.0, or 1.3-1.9. In some embodiments, the crude product has an MCR content that is a maximum of 90%, 80%, 50% or maximum 10% of the MCR content of the crude feed. In some embodiments, the crude product has an MCR content in the range of 1 to 80%, 10 to 70%, 20 to 60%, or 30 to 50% of the MCR content of the crude feed. In some embodiments , the crude product has 0.0001 to 0.1 grams, 0.005 to 0.08 grams, or 0.01 to 0.05 grams of MCR per gram of raw product. In certain aspects, the product includes from more than O grams, but less than 0.01 grams, 0.000001-0.001 grams, or 0.00001-0.0001 grams of total catalyst per gram of crude product. The catalyst can serve to stabilize the crude product during transportation or treatment. The catalyst can inhibit corrosion, friction or increase the water separation capacity of the crude product. The methods that were described herein can be configured to add one or more catalysts described herein to the raw product during the treatment. The crude product produced from the contact system 100 has properties different from the properties of the crude feed. Such properties may include, but not limited to: a) TAN reduced; b) reduced viscosity; c) total content of reduced Ni / V / Fe; d) content of sulfur, oxygen, nitrogen or its reduced combinations; e) reduced waste content; f) reduced C5 asphaltene content; g) reduced MCR content; h) higher API gravity; i) content of metals in metal salts of reduced organic acids; or j) combinations thereof. In certain embodiments, one or more properties of the crude product, relative to the crude feed, can be changed selectively while not changing other properties too much or not substantially. For example, it may be desirable to selectively reduce only the TAN index in a crude feed without significantly changing the amount of other components (eg, sulfur, residue, Ni / V / Fe, or VGO). In this way, the uptake of hydrogen can be "concentrated" during contact with the reduction of the TAN and not with the reduction of other components. Therefore, the TAN index of the crude feed can be reduced, while less hydrogen is used, since less of such hydrogen is also used to reduce other components in the crude feed. If, for example, the disadvantageous crude has a high TAN index, but the sulfur content is acceptable to meet the specifications for treatment or transportation, then such crude feed can be treated more efficiently to reduce the TAN index without reducing also sulfur. The catalysts used in one or more embodiments of the inventions may include one or more crude metals or one or more metals on the base. The metals may be in elemental form or in the form of a metal compound. The catalyst described herein can be introduced into the contact zone as a precursor, and then activated as a catalyst in the contact zone (for example, when sulfur and / or sulfur-containing crude feed is contacted with the precursor).

The catalyst or combination of catalysts used as described herein may or may not be commercial catalysts. Examples of commercial catalysts that are contemplated for use herein as described include: HDS3; HDS22; HDN60; C234; C311; C344; C411; C424; C344; C444; C447; C454; C448; C524; C534; DN110; DN120; DN130; DN140; DN190; DN200; DN800; DN2118; DN2318; DN3100; DN3110; DN3300; DN3310; RC400; RC410; RN412; RN400; RN420; RN440; RN450; RN650; RN5210; RN5610; RN5650; RM430; RM5030; Z603; Z623; Z673: Z703; Z713; Z723; Z753; and Z763, which are available from CRI International. Inc. (Houston, Texas, USA). In some embodiments, the catalysts used to change the properties of the crude feed include one or more metals from Columns 5 to 10 on the base. The metals of Columns 5 to 10 include, but are not limited to, vanadium, chromium, molybdenum, tungsten, manganese, tecnetium, rhenium, iron, cobalt, nickel, ruthenium, palladium, rhodium, osmium, iridium, platinum, or mixtures of the same. The catalyst may have, per gram of catalyst, a total metal content of Columns 5-10 metal (s) of at least 0.0001 grams, at least 0.001 grams, 0.01 grams or in the range of 0.0001-0.6 grams, 0.005- 0.3 grams, 0.00 1-0.1 grams, or 0.01-0.08 grams. In some embodiments, the catalyst includes the elements of column 15 in addition to the metals of columns 5 to 10. Examples of elements of Column 15 include phosphorus. The catalyst may have a total content of the element of column 15, per gram of catalyst, which is in the range of 0.00000 1 to 0.1 grams, 0.00001 to 0.06 grams, 0.00005 to 0.03 grams, or 0.000 1 to 0.001 grams. In certain embodiments, the catalyst includes metals from column 6. The catalyst may have, per gram of catalyst, a total metal content of columns 6 of at least 0.0001 grams, at least 0.01 grams, at least 0.02 grams or at range of 0.0001-0.6 grams, 0.005-0.3 grams, 0.001-0.3 grams, 0.005 to 0.1 grams, or 0.01-0.08 grams. In some embodiments, the catalyst includes from 0.0001 to 0.06 grams of metals from column 6 per gram of catalyst. In some embodiments, the catalyst includes the elements of column 15 in addition to the metals of columns 6. In some embodiments, the catalyst includes a combination of the metals in column 6 with one or more metals in column 5 and / or from columns 7 to 10. The molar ratio of the metal in column 6 and column 5 can be found in the range of 0.1 to 20. 1 to 10, or 2 to 5. The molar ratio of the metal in column 6 and of the metal of columns 7 to 10 may be in the range of 0.1 to 20, 1 to 10, or 2 to 5. In some embodiments, the catalyst includes the elements of column 15 in addition to the combination of the metals in the column 6 with one or more metals from columns 5 and / or 7-10. In other embodiments, the catalyst includes metals from column 6 and metals from column 10. The molar ratio of the total metal of column 10 to the total metal of column 6 in the catalyst may be in the range of 1- 10, or 2-5. In certain embodiments, the catalyst includes metals from column 5 and metals from column 10. The molar ratio of the total metal of column 10 and the total metal of column 5 in the catalyst can be in the range of 1- 10, or 2-5. In certain embodiments the catalyst includes the metals of column 5 and the metals of column 10. The molar ratio of the total metal of column 10 to the total metal of column 5 in the catalyst may be in the range of 1. -10, or 2-5. In some embodiments, the metals in columns 5 to 10 are incorporated, or deposited in a base to form the catalyst. In certain modalities, the metals of columns 5 to 10, combined with the elements of column 15 are incorporated, or deposited on a base to form the catalyst. In embodiments in which metals or elements are supported, the weight of the catalyst includes all bases, all metals and all elements. The base may be porous and may include refractory oxides, porous carbon based materials, zeolites, or combinations thereof. The refractory oxides may include, but are not limited to, alumina, silica, silica-alumina, titanium oxide, zirconium oxide, magnesium oxide, or mixtures thereof. The bases can be obtained from a commercial manufacturer such as Criterion Catalysts and Technologies LP (Houston, Texas, USA). The porous carbon-based materials include, but are not limited to, activated carbon and / or porous graphite. Examples of zeolites include Y zeolites, beta zeolites, mordenite zeolites, ZSM-5 zeolites and ferrierite zeolites. The zeolites can be obtained from a commercial manufacturer such as Zeolyst (Valley Forge, Pensilvana, USA). In some embodiments the base is prepared so that it has an average pore diameter of at least 150 A, at least 170 A, or at least 180 A. In certain embodiments, the base is prepared by forming an aqueous paste of the base material. In some embodiments, acid is added to the paste to allow extrusion of the paste. Water and dilute acid are added in such amounts and by such methods as required to give the extrudable paste in a desired consistency. Examples of acids include, but are not limited to, nitric acid, acetic acid, sulfuric acid, and hydrochloric acid. Extrusion of the pulp can be done, and can be cut using generally known catalyst extrusion methods and catalyst cutting methods to form extrudates. The extrudates can be heat treated at the temperature in the range of 5-260 ° C or 85-235 ° C for a period of time (for example, for 0.5 to 8 hours) or until the moisture content of the extrudate has reached the desired levels. The heat-treated extrudate can be further treated with heat at a temperature in the range of 800-1200 ° C or 900-1100 ° C to form a base with an average pore diameter of at least 150 A. In certain embodiments, the base includes range alumina, theta alumina, delta alumina, alpha alumina or combinations thereof. The amount of range alumina, delta alumina, alpha alumina or combinations thereof per gram of catalyst base, can be in the range of 0.0001 to 0.99 grams, 0.001 to 0.5 grams, 0.01 to 0.1 grams or 0.1 grams maximum as determined by x-ray diffraction. In some embodiments, the base has, either alone or in combination with other forms of alumina, a content of theta alumina, per gram of base, in the range of 0.1 to 0.9 grams, 0.5 to 0.9 grams, or 0.6 to 0.8 grams , as determined by X-ray diffraction. In certain embodiments, the base may have at least 0.1 grams, at least 0.3 grams, at least 0.5 grams or at least 0.8 grams of theta alumina, as determined by light scattering. X. The base catalysts can be prepared using generally known catalyst preparation techniques. Examples of catalyst preparations are described in North American patents: 6,218,333 by Gabrielov et al.; 6,290,841 to Gabrielov et al .; and 5,744,025 to Boon et al., and U.S. Patent Application Publication No. 20030111391 to Bhan.

In certain embodiments, the base may be impregnated with metal to form a catalyst. In certain embodiments, the base is heat treated at temperatures in the range of 400-1200 ° C, 450-1000 ° C, or 600-900 ° C before impregnation with a metal. In certain embodiments, substances that assist in impregnation can be used during the preparation of the catalysts. Examples of substances that assist in impregnation include a component of citric acid, ethylenediaminetetraacetic acid (EDTA), ammonia, or mixtures thereof. In certain embodiments, a catalyst can be formed by the addition or incorporation of metals from columns 5 to 10 into mixtures formed with heat treatment of base ("coating"). The coating of a metal on the base formed with heat treatment having a relatively or substantially uniform concentration of metal, often provides beneficial catalyst catalytic properties. The heat treatment of a base formed after each metal coating tends to improve the catalytic activity of the catalyst. Methods for preparing the catalyst using coating methods are described in U.S. Patent Application Publication No. 20030111391 to Bhan. The metals from column 5 to 10 and the base can be mixed with suitable mixing equipment to form the base / metal mixture of columns 5 to 10. The base / metals mixture of columns 5 to 10 can be mixed using a suitable mixing equipment. Examples of suitable mixing equipment include stationary drums, cylinders or buckets, Muller mixers (eg, batch or continuous), impact mixers, or any other generally known mixer or device, that adequately provide the mix of base / metals of column 5 to 10. In certain embodiments, the materials are mixed until the metals of columns 5 to 10 are dispersed substantially homogeneously in the base. In some embodiments, the catalyst is treated with heat at temperatures from 150-750 ° C, from 200 to 740 ° C, or from 400 to 730 ° C after combining the base with the metal. In some embodiments, the catalyst may be heat treated in the presence of hot air or air enriched with oxygen at a temperature in the range of 400 ° C to 1000 ° C to remove the volatile material such that at least a portion of the metals in columns 5 to 10 are converted to corresponding metal oxide. However, in other embodiments, the catalyst may be heat treated in the presence of air at temperatures in the range of 35 to 500 ° C (e.g., below 300 ° C, below 400 ° C or below 500 ° C). ° C) for a period of time ranging from 1 to 3 hours to remove most of the volatile components without converting the metals from columns 5 to 10 into metal oxide. In general, the catalysts prepared by such a method are referred to as "uncalcined" catalysts. When the catalysts are prepared in this manner in combination with a sulfidation method, the active metals can be dispersed substantially in the base. Preparations of such catalysts are described in the following US Patent Nos: 6,218,333 to Gabrielov et al., And 6,290,841 to Gabrielov et al. In certain embodiments, the theta alumina base can be combined with the metals of columns 5 to 10 to form the mixture of metals from columns 5 to 10 / base theta alumina. The metal mixture of columns 5 to 10 / base of theta alumina can be heat treated at temperatures of at least 400 ° C to form the catalyst having a pore size distribution with a mean pore diameter of at least 230 ° C. . In general, such heat treatment is carried out at temperatures of maximum 1200 ° C. In some embodiments, the base (either commercial base or prepared base as described herein) may be combined with a catalyst with base or with a crude metal catalyst. In some embodiments, the base catalyst may include metals from column 15.

For example, the catalyst with base or the crude metal catalyst can be fractionated to form powders with an average particle size of 1 to 50 microns, 2 to 45 microns or 5 to 40 microns. The powder can be combined with the base to form an embedded metal catalyst. In some embodiments, the powder can be combined with the base and then then extrusion performed with standard techniques to form a catalyst with a pore size distribution with a mean pore diameter in the range of 80-200 A or 90-180 A , or 120-130 Á. The combination of the catalyst with the base allows, in some embodiments, that at least a portion of the metal remain below the surface of the embedded metal catalyst (e.g., embedded in the base), which leads to less metal on the surface than otherwise it would occur in the non-embedded metal catalyst. In some embodiments, having less metal on the surface of the catalyst prolongs the life or catalytic activity of the catalyst, allowing at least a portion of the metal to travel to the surface of the catalyst during use. The metals can be displaced to the catalyst surface by erosion of the catalyst surface during contact with the crude feed. The intercalation or mixing of the catalyst components changes, in some embodiments, the structured order of the metal in column 6 in the oxide crystal of column 6, to give substantially random order of the metal in column 6 in the structure of the column. crystal of the embedded catalyst. The metal order of column 6 can be determined with dust x-ray diffraction methods. The order of the elemental metal in the catalyst relative to the order of the elemental metal in the metal oxide can be determined by comparing the order of the metal peak of column 6 in a x-ray diffraction spectrum of the oxide of column 6 with the order of the metal peak of column 6 in the x-ray diffraction spectrum of the catalyst. From the enlargement or absence patterns associated with a metal of column 6 in the x-ray diffraction spectrum, it is possible to estimate that the metals in column 6 are randomly arranged randomly in the crystal structure. For example, the base of molybdenum trioxide and alumina having a mean pore diameter of at least 180A can be combined to form a mixture of alumina / molybdenum trioxide. Molybdenum trioxide has a definite pattern (for example, definitive peaks of D0o ?, D0o2 and / or D0o3) • The alumina / trioxide mixture of column 6 can be treated with heat at a temperature of at least 538 ° C ( 1000 ° F) to produce a catalyst that does not exhibit the pattern of molybdenum dioxide in an x-ray diffraction spectrum (eg, absence of the D0o? Peak) - In some embodiments, the catalysts can be characterized by the pore structure. The parameters of the pore structure include, but are not limited to, the pore diameter, pore volume, surface areas, or combinations thereof. The catalyst may have a distribution of the total amount of pore size versus the pore diameter. The average pore diameter of the pore size distribution can be in the range of 30-1000 A, 50-500 A, or 60-300 A. In some embodiments, the catalysts include at least 0.5 grams of gamma alumina per gram of catalyst have a pore size distribution with a mean pore diameter in the range of 60-200 A; 90-180 A, 100-140 A, or 120-130 A. In other embodiments, catalysts that include at least 0.1 gram of theta alumina per gram of catalyst have a pore size distribution with a mean pore diameter in the interval of 180-500 Á, 200-300 Á, or 230-250 Á. In some embodiments, the average pore diameter of the pore size distribution is at least 120 Á, at least 150 A, at least 180 A, at least 200 A, at least 220 A, at least 230 A, or at least 300 A. Such average pore diameters are generally of maximum 1000 Á. The catalyst may have a pore size distribution with an average pore diameter of at least 60 A or at least 90 A. In certain embodiments, the catalyst has a pore size distribution with an average pore diameter in the range of 90-180 A, 100r140 A, or 120-130 A, with at least 60% of the total number of pores in the pore size distribution having a pore diameter of 45 A, 35 A, or 25 A of the average pore diameter. In certain embodiments, the catalyst has a pore size distribution with a mean pore diameter in the range of 70 to 180 A, with at least 60% of the total number of pores in the pore size distribution having a diameter of pore of 45 A, 35 A, or 25 A of the average pore diameter. In embodiments in which the average pore diameter of the pore size distribution is at least 180 A, at least 200 A, or at least 230 A, more than 60% of the total number of pores in the pore size distribution , has a diameter of 50 A, 70 A, or 90 A of the average pore diameter. In certain embodiments, the catalyst has a pore size distribution with a mean pore diameter in the range of 180-500 A, 200-400 A, or 230-300 A, with at least 60% of the total number of pores in the range. the pore size distribution having a pore diameter of 50 A, 70 A, or 90 A of the average pore diameter. In some embodiments, the pore volume can be at least 0.3 cm3 / g, at least 0.7 cm3 / g or at least 0.9 cm3 / g. In certain embodiments, the pore volume of the pores may be in the range of 0.3-0.99 cm3 / g, 0.4-0.8 cm3 / g, or 0.5-0.7 cm3 / g. The catalyst having a pore size distribution with a mean pore diameter in the range of 90-180 Á can, in some embodiments, have a surface area of at least 100 m2 / g, 120 m2 / g, 170 m2 / g, at least 220 or at least 270 m2 / g. Such surface area may be in the range of 100-300 m2 / g, 120-270 m2 / g, 130-250 m2 / g, or 170-220 m2 / g. In certain embodiments, the catalyst having a pore size distribution with a mean pore diameter in the range of 180-300 A may have a surface area of at least 60 m2 / g, 90 m2 / g, 100 m2 / g, 120 m2 / g, or at least 270 m / g. Such surface area may be in the range of 60-300 m2 / g, 90-280 m2 / g, 100-270 m2 / g, or 120-250 m / g. In certain embodiments, the catalyst exists in defined forms, e.g., pills, cylinders or extrusion products. Typically the catalyst has a flat plate fraction strength in the range of 50-500 N / cm, 60-400 N / cm, 100-3 50 N / cm, 200-300 N / cm, or 220-280 N / cm In some embodiments, the catalyst or catalyst precursor is sulfided to form metal sulfides (before use) using techniques known in the art (eg, ACTICAT ™ process, CRI International, Inc.). In some embodiments, the catalyst can be dried and then sulfurized. Alternatively, the catalyst can be sulfided in situ by contacting the catalyst with a crude feed including sulfur-containing compounds. Sulfurization in situ can use either gaseous hydrogen sulfide in the presence of hydrogen, or liquid phase sulfurization agents such as organosulfur compounds (including alkylsulfides, polysulfides, thiols, and sulfoxides). Ex situ sulfurization processes are described in US Pat. Nos .: 5,468,372 to Seamans et al., And 5,688,736 to Seamans et al. In certain embodiments, a first type of catalyst ("first catalyst") includes metals from columns 5 to 10. in combination with a base, and have a pore size distribution with a mean internal pore diameter of 150 to 250 A. The first catalyst can have a surface area of at least 100 m2 / g. The pore volume of the first catalyst can be at least 0.5 cm 3 / g. The first catalyst can have an alumina content of at least 0.5 grams of alumina range and generally of maximum 0.9999 grams of alumina range per gram of first catalyst. In some embodiments the first catalyst has a total metal content of column 6 per gram of catalyst, in the range of 0.0001 to 0.1 grams. The first catalyst is capable of removing a portion of Ni / V / Fe. of the crude feed, elimination of a portion of components that contribute to the TAN index of the crude feed, elimination of at least a portion of C5 asphaltenes from the crude feed, elimination of at least a portion of the metals in metal salts of organic acids in the crude feed, or combinations thereof. Other properties (eg, sulfur content, VGO content, API gravity, waste content, or combinations thereof) may exhibit relatively small changes when the crude feed is contacted with the first catalyst. The ability to selectively change the properties of the crude feed while only changing other properties in relatively small amounts, may allow to more efficiently treat the crude feed. In some embodiments, one or more of the first catalysts may be used in any order. In certain embodiments, the second type of catalyst ("second catalyst") includes the metals of columns 5 to 10 combined with the base, and have a pore size distribution with a mean pore diameter in the range of 90 A to 180 A. At least 60% of the total number of pores in the pore size distribution of the second catalyst has a pore diameter of 45 A of the average pore diameter. The contact of the crude feed with the second catalyst under suitable contact conditions can produce a crude product having selected properties (for example, the TAN index) significantly changed relative to the same properties of the crude feed, while the others Properties change only in small quantities. In some embodiments the source of hydrogen may be present during contact. The second catalyst can reduce at least a portion of the components contributing to the TAN index of the crude feed, at least a portion of the components contributing to relatively high viscosities, and reduce at least a portion of the Ni / V / content. Fe of the crude product. Furthermore, the contact of the crude feeds with the second catalyst can produce the crude product with a change in the relatively small sulfur content with respect to the sulfur content of the crude feedstock. For example, the crude product may have a sulfur content of 70% to 130% of the sulfur content of the crude feed. The raw product may also exhibit relatively small changes in the distillate content, VGO content, and the residue content relative to the crude feed. In some embodiments, the crude feed may have a relatively low Ni / V / Fe content (eg, maximum 50 wtppm), but a TAN index, asphaltene content, or metal content in metal salts of relatively high organic acids . A relatively high TAN index (for example, a TAN index of at least 0.3) can result in a crude feed that is not acceptable for transportation or refining. A disadvantageous crude with a relatively high Cs asphaltene content may exhibit less stability during processing relative to other crudes with a relatively low C5 asphaltene content. The contact of the crude feed with the second catalyst can eliminate the acidic components or C5 asphaltenes that contribute to the TAN index of the crude feed. In some embodiments, the reduction of C5 asphaltenes or of the components contributing to the TAN index may reduce the viscosity of the crude feed / total product mixture relative to the viscosity of the crude feed. In certain embodiments, one or more combinations of second catalysts may improve the stability of the product / total product mix, increase the life of the catalyst, allow a minimum net hydrogen uptake by the crude feed, or combinations of these, when used to treat the crude feed as described herein. In some embodiments, the third type of catalyst ("third catalyst") can be obtained by combining a base with the metals of column 6 to produce a catalyst precursor. The catalyst precursor may be heated in the presence of one or more sulfur-containing compounds at a temperature below 500 ° C (e.g., below 482 ° C) for a relatively short period of time to form the third catalyst without calcining . In general, the catalyst precursor is heated to at least 100 ° C for 2 hours. In certain embodiments, the third catalyst may have, per gram of catalyst, an element content of column 15 in the range of 0.001 to 0.03 grams, 0.005 to 0.02 grams or 0.008 to 0.01 grams. The third catalyst can exhibit significant activity and stability when used to treat the crude feed as described herein. In some embodiments, the catalyst precursor is heated to temperatures below 500 ° C in the presence of one or more sulfur compounds. The third catalyst can reduce at least a portion of the components that contribute to the TAN index of the crude feed, reduce at least a portion of the metals in the metal salts of organic acids, reduce the Ni / V / Fe content of the crude product, and reduce the viscosity of the crude product. In addition, the contact of the crude feeds with the third catalyst can produce a crude product with a change in the relatively small sulfur content relative to the sulfur content of the crude feed and relative to the minimum net hydrogen uptake by the feed of raw. For example, the crude product may have a sulfur content of 70% to 130% of the sulfur content of the crude feed. The crude product produced using the third catalyst may also exhibit relatively small changes in API gravity, distillate content, VGO content, and residue content relative to crude feed. The ability to reduce the TAN index, metals in metallic salts of organic salts, Ni / V / Fe content and viscosity of the crude product while also only changing API gravity, distillate content, VGO content, in only small amounts, and waste content relative to the crude feed, may allow the crude product to be used in a variety of treatment facilities. In some embodiments, the third catalyst can reduce at least a portion of the MCR content of the crude feed, while maintaining the stability of the crude feed / total product. In certain embodiments, the third catalyst may have a metal content of column 6 in the range of 0.0001-0.1 grams, 0.005-0.05 grams, or 0.001-0.11 grams and a metal content of column 10 in the range of 0.0001 -0.05 grams, 0.005-0.03 grams, or 0.001-0.01 grams per gram of catalyst. The metal catalyst of columns 6 and 10 can facilitate the reduction of at least a portion of the components contributing to the MCR in the crude feed at temperatures in the range of 300-500 ° C or 350-450 ° C and pressures in the range of 0.1-10 MPa, 1-8 MPa, or 2-5 MPa. In certain embodiments, the fourth type of catalyst ("fourth catalyst") includes metals from column 5 in combination with a base of theta alumina. The fourth catalyst has a pore size distribution with a mean pore diameter of at least 180 Á. In some embodiments, the average pore diameter of the fourth catalyst may be at least 220 A, 230 A, 250 A, 300 A. The base may include at least 0.1 grams, 0.5 grams, 0.8 grams, or at least 0.9 grams of theta alumina per gram of base. The fourth catalyst may include, in some embodiments, maximum 0.1 grams of metals from column 5 per gram of catalyst, and at least 0.0001 grams of metals from column 5 per gram of catalyst. In certain embodiments, the metal in column 5 is vanadium.

In some embodiments, the crude feed may be contacted with an additional catalyst subsequent to contact with the fourth catalyst. The additional catalyst may be one or more of the following: the first, second, third, fifth, sixth, seventh catalyst, commercial catalysts described herein, or combinations thereof. In some embodiments, hydrogen can be generated during the contact of the crude feed with the fourth catalyst at temperatures in the range of 300-400 ° C, 320-380 ° C, or 330-370 ° C. The raw product produced from such contact can have a TAN index of maximum 90%, 80%, 50%, or maximum 10% of the TAN index of the crude feed. Hydrogen generation can range from 1-50 Nm3 / m3, 10-40 Nm3 / m3, or 15-25 Nm3 / m3. The crude product can have a content of Ni / V / Fe of maximum 90%, 80%, 70% or maximum 50%, maximum 10% or at least 1% of the total content of Ni / V / Fe of the crude feed . In certain embodiments, the fifth type of catalyst ("fifth catalyst") includes metals from column 6 in combination with a theta alumina base. The fifth catalyst has a pore size distribution with a mean pore diameter of at least 180 Á, 220 Á, 230 Á, 250 Á, 300 Á, or at least 500 Á. The base may include at least 0.1 grams, 0.5 grams or maximum 0.999 grams of theta alumina per gram of base. In some embodiments, the base has an alpha alumina content below 0.1 gram of alpha alumina per gram of catalyst. The catalyst may include, in some embodiments, maximum 0.1 grams of metals from column 6 per gram of catalyst, and at least 0.0001 grams of metals from column 6 per gram of catalyst. In some embodiments, the metals in column 6 are molybdenum or tungsten. In certain embodiments, the uptake of net hydrogen by the crude feed may be relatively low (for example from 001-100 Nm3 / m3, 1-80 Nm3 / m3, 5-50 Nm3 / m3, or 10-30 Nm3 / m3 ) when the crude feed is contacted with the fifth catalyst at temperatures in the range of 310-400 ° C, 320-370 ° C, or from 330-360 ° C. In some embodiments, the uptake of net hydrogen by the crude feed may be in the range of 1-20 Nm3 / m3, 2-15 Nm3 / m3, or 3-10 Nm3 / m3. The crude product produced from the contact of the crude feed with the fifth catalyst can have a TAN index of maximum 90%, 80%, 50% or maximum 10% of the TAN index of the crude feed. The TAN index of the crude product can be in the range of 0.01-0.1, 0.03-0.05, or 0.02-0.03. In certain embodiments, the sixth type of catalyst ("sixth catalyst") includes metals from column 5 and column 6 in combination with a theta alumina base. The sixth catalyst has a pore size distribution with a mean pore diameter of at least 180 A. In some embodiments, the average pore diameter of the pore size distribution can be at least 220 A, minus 230 A, 250 A, 300 Á, or at least 500 A. The base may include at least 0.1 grams, 0.5 grams, 0.8 grams, or at least 0.9 grams, or maximum 0.99 grams of theta alumina per gram of base. In some embodiments the catalyst may include a total of metal from column 5 and from column 6 of maximum 0.1 grams per gram of catalyst, and at least 0.0001 grams of metals from column 5 and from column 6 per gram of catalyst. In some embodiments, the molar ratio of the total metal of column 6 and the total metal of column 5 may be in the range of 0.1-20, 1-10, or 2-5. In certain embodiments, the metal in column 5 is vanadium and the metals in column 6 are molybdenum or tungsten. When the crude feed is contacted with the sixth catalyst at temperatures in the range of 310-400 ° C, 320-370 ° C, or 330-360 ° C, the net hydrogen uptake by the crude feed it can be in the range of -10 Nm3 / m3 to 20 Nm3 / m3, -7 Nm3 / m3 at 10 Nm3 / m3, or -5 Nm3 / m3 at 5 Nm3 / m3. The net negative hydrogen uptake is indicative of hydrogen generation in situ. The crude product produced from the contact of the crude feed with the sixth catalyst can have a TAN index of maximum 90%, 80%, 50% or maximum 10%, or at least 1% of the TAN index of the crude feed. The TAN index of the crude product may be in the range of 0.01-0.1, 0.02-0.05, or 0.03-0.04. The low uptake of net hydrogen during contact of the crude feed with the fourth, fifth or sixth catalyst reduces the total hydrogen requirement during processing, while producing a crude product that is acceptable for transportation and / or treatment. Since the production and / or transportation of hydrogen is expensive, minimizing the use of hydrogen in the process decreases the total processing costs. In certain embodiments a seventh type of catalyst (seventh catalyst) has a total metal content of column 6 in the range of 0.000 1 to 0.06 grams of metals from column 6 per gram of catalyst. The metal in column 6 is molybdenum and / or tungsten. The seventh catalyst is beneficial to produce a crude product having a TAN index of maximum 90% of the TAN index of the crude feed. Other embodiments of the first, second, third, fourth, fifth, sixth and seventh catalyst may also be made and / or used as described otherwise herein.

The selection of the catalysts of this application, and the control of the operating conditions, may allow producing the crude product that has a TAN index and / or selected properties changed in relation to the crude feed, while the other products are not changed significantly. properties of crude feed. The resulting crude product can _. have improved properties relative to the crude feed, and thus, be more acceptable for transport and / or refinement. If two or more catalysts are organized in a selected sequence, the sequence of property improvements for the crude feed can be controlled. For example, the TAN index, the API gravity, at least a portion of the C5 asphaltenes, at least a portion of the iron, at least a portion of niguel, or at least a portion of vanadium in the crude feed, can be decreased before reducing at least a portion of the heteroatoms in the crude feed. The arrangement and / or selection of the catalysts can, in certain embodiments, improve the life of the catalysts and / or the stability of the crude feed mixture and / or total product. By improving catalyst life and / or stability of the crude feed mixture and / or total product during processing, the contact system can be allowed to operate for at least 3 months, at least 6 months, or at least 1 year without replacing the catalyst in the contact zone. The combinations of selected catalysts can allow the reduction in at least a portion of Ni / V / Fe, at least a portion of the asphaltenes C5, at least a portion of the metals in metal salts of organic acids, at least a portion of the components that contribute to the TAN index, at least a portion of the waste, or combinations thereof, of the crude feed before other properties of the crude feed are changed, while maintaining the stability of the crude feed mix / total product during processing (for example, maintaining a P value of the crude feed above 1.5). Alternatively, C5 asphaltenes, TAN index or API gravity can be decreased more and more by contacting the crude feed with the selected catalysts. The ability to change the properties of the crude feed extensively or selectively may allow the stability of the raw feed mix / total product to be maintained during processing. In some embodiments, the first catalyst (described above) can be placed upstream of a series of catalysts. Such a position of the first catalyst can allow the removal of high molecular weight contaminants, metal contaminants, and / or metals in metal salts of organic acids, while maintaining the stability of the raw / total product feed mixture. In some embodiments, the first catalyst allows the removal of at least a portion of the Ni / V / Fe, the removal of the acid components, removal of the components that contribute to decrease the life of other catalysts in the system, or combinations of the same, of the crude feed. For example, the reduction of at least a portion of the C5 asphaltenes in the crude feed / total product mixture relative to the crude feed inhibits the connection of other catalysts that are downstream, and therefore, increase the length of time in which the contact system can operate without catalyst replenishment. In some embodiments, the removal of at least a portion of Ni / V / Fe from the crude feed may increase the life of one or more catalysts located after the first catalyst. The second and / or third catalyst can be placed downstream of the first catalyst. In addition the contact of the raw feed mix / total product with the second catalyst and / or third catalyst can further reduce the reduced TAN index, reduced Ni / V / Fe content, reduced sulfur content, reduced oxygen content, reduced metal content in metallic salts of organic acids. In some embodiments, contacting the crude feed with the second catalyst and / or the third catalyst can produce a crude feed / total product mixture having a reduced TAN index, a reduced sulfur content, a reduced oxygen content , a reduced content of metals in metallic salts of organic acids, a reduced asphaltenes content, a reduced viscosity, or combinations of the same, relative to the respective properties of the crude feed -while maintaining the stability of the crude feed mix / total product during processing. The second catalyst can be located in series, either the second catalyst that is upstream of the third catalyst, or vice versa. The ability to release hydrogen in specific contact zones tends to minimize the use of hydrogen during contact. Combinations of catalysts that facilitate the generation of hydrogen during contact, and catalysts that capture a relatively small amount of hydrogen during contact, can be used to change the selected properties of the crude product relative to the same properties of the crude feed. . For example, the fourth catalyst can be used in combination with the first catalyst, second catalyst, third catalyst, fifth catalyst, sixth catalyst, and / or seventh catalyst to change the selected properties of a crude feed, while changing only the other properties of the crude feed by selected quantities, and / or while maintaining the stability of the crude feed / total product. The order and / or number of the catalysts can be selected to minimize the uptake of net hydrogen while maintaining the stability of the total product / crude feed. Minimum net hydrogen uptake allows to maintain the content of the residue, VGO content, distillate content, API gravity, or combinations thereof of the crude feed within 20% of the respective properties of the crude feed, while the TAN index and / or the viscosity of the crude product is maximum 90% of the TAN index and / or viscosity of the crude feed. The reduction of the net hydrogen uptake by the crude feed allows to produce a crude product that has a distribution in the boiling range similar to the boiling point distribution of the crude feed, and a reduced TAN index in relation with the TAN index of the crude feed. The atomic ratio H / C of the crude product can also change only in relatively small amounts in comparison as compared to the atomic ratio H / C of the crude feed. The generation of hydrogen in specific contact zones can allow the selective addition of hydrogen to other contact zones, and / or allow the selective reduction of the properties of the crude feed. In some embodiments, the fourth catalysts can be located upstream, downstream or between 1 additional catalysts described herein. Hydrogen can be generated during the contact of the crude feed with the fourth catalyst, and hydrogen can be released to the contact zone including the additional catalysts. The release of hydrogen may be contrary to the flow of the crude feed. In some embodiments, hydrogen release may be concurrent with the flow of the crude feed. For example, in a stacked configuration (see, eg, FIG. 2B), hydrogen can be generated during contact in a contact zone (eg, contact zone 102 of FIG. 2B), and hydrogen can be released in other contact areas (e.g., contact zone 114 in Figure 2B) in a direction that is contrary to the flow of the crude feed. In some embodiments, the flow of hydrogen may be concurrent with the flow of the crude feed. Alternatively, in a stacked configuration (see, for example, Figure 3B), hydrogen can be generated during contact in a contact zone (e.g., contact zone 102 in Figure 3B). A source of hydrogen can be released to a first additional contact zone in a direction that is contrary to the flow of the crude feed (eg, by adding hydrogen through conduit 106 'to contact zone 114 in Figure 3B), and to a second additional contact zone in a direction that is concurrent with the flow of the crude feed (eg, by adding hydrogen through conduit 106 'to contact zone 116 in Figure 3B). In certain embodiments, the fourth and sixth catalysts are used in series, either the fourth catalyst upstream of the sixth catalyst, or vice versa. The combination of the fourth catalyst with an additional catalyst can reduce the TAN index, Ni / V / Fe content, and / or reduce the metal content in metal salts of organic acids, with lower net hydrogen uptake by the crude feed. . The low uptake of net hydrogen may allow other properties of the crude product to change only in small amounts relative to the same properties of the crude feed. In certain embodiments, two different seventh catalysts can be used in combination. The seventh catalyst used upstream from the seventh downstream catalyst may have a total metal content of column 6, per gram of catalyst, in the range of 0.0001 to 0.06 grams. The seventh downstream catalyst may have a total metal content of column 6, per gram of seventh downstream catalyst, which is equal to or greater than the total metal content of column 6 in the seventh upstream catalyst, or at least 0..02 grams of metals from column 6 per gram of catalyst. In some embodiments, the position of the seventh catalyst upstream and the seventh downstream catalyst can be reversed. The ability to use a relatively small amount of catalytically active metal in the seventh downstream catalyst may allow other properties of the crude product to be changed only in small amounts relative to the same properties of the crude feed (eg, a relatively small change in content). of heteroatoms, API gravity, waste content, VGO content, or combinations thereof). The contact of the crude feed with the seventh catalysts upstream and downstream can produce a crude product that has a TAN index of maximum 90%, 80%, 50%, maximum 10%, or at least 1% of the TAN index of the crude feed. In certain embodiments, the TAN index of the crude feed can be greatly reduced by contact with the seventh catalysts upstream and downstream (eg, contacting the crude feed with a catalyst to form a crude initial product with relative changed properties). to the crude feed, and then contact the raw initial product with an additional catalyst to produce the crude product with changed properties relative to the crude initial product). The ability to reduce the TAN index extensively can help maintain the stability of the total product / crude feed mix during processing. In some embodiments, the selection of the catalyst, and / or the order of the catalysts in combination with the controlled contact conditions (eg, temperature and / or flow rate of the crude feed) can help reduce the uptake of hydrogen by feeding crude, maintaining the stability of the total product / crude feed mix during processing, and changing one or more properties of the crude product relative to the respective properties of the crude feed. The stability of the total product / crude feed mix can be affected by various separation phases of the total product / crude feed mix. For example, the phase separation can be caused by the insolubility of the crude feed and / or the crude product in the raw feed mix / total product, the flocculation of the asphaltenes of the total product mix / raw feed , precipitation of the components of the crude feed mix / total product, or combinations thereof. At certain times during the contact period, you can change the crude feed concentration and / or total product in the raw / total product feed mix. As the concentration of total product in the total product / crude feed mix changes due to the formation of crude product, it tends to change the solubility of the raw feed components and / or the total product components in the mixture of total product / crude feed. For example, the crude feed may contain components that are soluble in the crude feed at the start of processing. As the properties of the crude feed change (for example, the TAN, MCR, asphaltenes C5, P value, or combinations thereof), the components tend to be less soluble in the crude feed / total product mix. In some instances, the crude feed and the total product may form two phases and / or become insoluble to each other. Changes in solubility can also result in the formation of two or more phases of the total product / crude feed mix. The formation of two phases, by the flocculation of asphaltenes, changes in the concentration of crude feed and total product, and / or the precipitation of the components, tend to reduce the life of one or more catalysts. In addition, it can decrease the efficiency of the process. For example, repeated treatment of the crude feed / total product mix may be necessary to produce a crude product with desired properties. During processing, the P value of the raw / total product feed mix can be monitored and the process stability, crude feed, and / or crude feed / total product mix can also be evaluated. In general, the P value that is of maximum 1.5 indicates that flocculation of the asphaltenes generally takes place from the crude feed. If initially the value P is at least 1.5, and such value P increases or is relatively stable during contact, then it indicates that the crude feed is relatively stable during contact. The stability of the total product / crude feed mixture, as evaluated by the P value, can be controlled by the contact condition controller, selecting the catalysts, selectively ordering the catalysts, or combinations thereof. Such control of contact conditions may include control of LHSV, temperature, pressure, hydrogen uptake, crude feed flow, or combinations thereof. In some embodiments, the contact temperatures are controlled such that the C5 and / or other asphaltenes are removed while the MCR content is maintained in the crude feed. Reducing the MCR content by hydrogen uptake or higher contact temperatures can result in the formation of two phases that can reduce the stability of the crude feed mix / total product and / or the life of one or more catalysts. The control of the contact temperatures and the uptake of hydrogen in combination with the catalysts described herein allows to reduce the C5 asphaltenes while only changing the MCR content of the crude source in relatively small amounts. In some embodiments, the contact conditions are controlled in such a way that the temperatures in one or more contact zones may be different. The operation at different temperatures allows a selective change of the properties of the crude feed while maintaining the stability of the crude feed mix / total product. The crude feed enters the first contact zone at the beginning of a process. A first contact temperature is the temperature in the first contact zone. Other contact temperatures (for example, the second temperature, third, fourth, etc.) are the temperatures in the contact zones that are located after the first contact zone. A first contact temperature may be in the range of 100-420 ° C, and a second contact temperature may be in the range of 20-100 ° C, 30-90 ° C, or 40-60 ° C different from the first contact temperature. In some embodiments, the second contact temperature is greater than the first contact temperature. Having different contact temperatures can reduce the content of the TAN / or asphaltene C5 index in a raw product relative to the content of the TAN index and / or asphaltenes Cs of the crude feed to a greater extent than the reduction in the quantity of the TAN index and / or asphaltenes C5, if any, when the first and second contact temperatures are equal or between each other are within 10 ° C. For example, the first contact zone may include a first catalyst, and / or a fourth catalyst, and a second contact zone may include other catalysts described herein. The first contact temperature can be 350 ° C and the second contact temperature can be 300 ° C. The contact of the crude feed in the first contact zone with the first catalyst and / or fourth catalyst at higher temperature before contact with the other catalyst in the second contact zone, may result in a greater reduction of the TAN index and C5 in the crude feed relative to the reduction of the TAN index and / or asphaltenes C5 in the same crude feed when the first and second contact temperatures are within 10 ° C.

EXAMPLES The following are examples of base preparation, catalyst preparations and systems with a selected arrangement of catalysts and controlled contact conditions.

Example 1. Preparation of a catalyst base. A base was prepared by grinding 576 grams of alumina (Criterion Catalysts and Technologies LP, Michigan City, Michigan, USA) with 585 grams of water and 8 grams of glacial nitric acid for 35 minutes. The resulting milled mixture was extracted with a Trilobe ™ 1.3 staining dish, dried between 90-125 ° C, and then calcined at 918 ° C, which resulted in 650 grams of calcined base with a diameter of average pore of 182 A. The calcined base was placed in a Lindberg oven. The oven temperature was raised to 1000-1100 ° C for 1.5 hours, and then held in this range for 2 hours to produce the base. The base includes 0.0003 grams of alumina range, 0.0008 grams of alpha alumina, 0.0208 grams of delta alumina, and 0.9781 grams of theta alumina per gram of base, as determined by X-ray diffraction. The base has a surface area of 110 m2 / g and a total pore volume of 0.821 cm3 / g. The base has a pore size distribution with an average pore diameter of 232 A, with 66.7% of the total number of pores in the pore size distribution having a pore diameter of 85 A of the average pore diameter. This example demonstrates how to prepare a base having a pore size distribution of at least 180 A and including at least 0.1 gram of theta alumina.

Example 2. Preparation of vanadium catalyst having a pore size distribution with a mean pore diameter of at least 230 A. The vanadium catalyst was prepared in the following manner. The alumina base, prepared by the method described Example 1, was impregnated with a vanadium impregnation solution prepared by the combination of 7.69 grams of VOS0 with 82 grams of deionized water. The pH of the solution was 2.27. The alumina base (100 g) was impregnated with the vanadium impregnation solution, allowed to stand for 2 hours with occasional stirring, dried at 125 ° C for a few hours, and calcined at 480 ° C for 2 hours. The resulting catalyst contained 0.04 grams of vanadium, per gram of catalyst, with the balance being the base. The vanadium catalyst has a pore size distribution with an average pore diameter of 350 A, a pore volume of 0.69 cm 3 / g, and a surface area of 110 m2 / g. In addition, 66.7% of the total number of pores in the pore size distribution of the vanadium catalyst has a pore diameter of 70 A of the average pore diameter. This example demonstrates the preparation of a column 5 catalyst having a pore size distribution with a mean pore diameter of at least 230 A.

Example 3. Preparation of molybdenum catalyst having a pore size distribution with a mean pore diameter of at least 230 A. The molybdenum catalyst was prepared in the following manner. The alumina base was prepared by the method described in Example 1 was impregnated with a molybdenum impregnation solution. The molybdenum impregnation solution was prepared by the combination of 4.26 grams of (NH) 2Mo207, 6.38 grams of Mo03, 1.12 grams of 30% H202, 0.27 grams of monoethanolamine (MEA), and 6.51 grams of deionized water to form a suspension. The suspension was heated to 65 ° C until the solids dissolved. The heated solution was cooled to room temperature. The pH of the solution is 5.36. The volume of the solution was adjusted to 82 ml of deionized water. The alumina base (100 g) was impregnated with the molybdenum impregnation solution, allowed to refuel for 2 hours with occasional stirring, dried at 125 ° C for several hours, and calcined at 480 ° C for 2 hours. The resulting catalyst contained 0.04 grams of molybdenum, per gram of catalyst, with the balance being the base. The molybdenum catalyst has a size distribution of per with an average pore diameter of 250 A, a pore volume of 0.77 cm3 / g, and surface area of 116 m2 / g. In addition, 67.7% of the total number of pores in the pore size distribution of the molybdenum catalyst has a pore diameter within 86 A of the average pore diameter. This example demonstrates the preparation of a metal catalyst of column 6 having a pore size distribution with a mean pore diameter of at least 230 A. Example 4. Preparation of molybdenum / vanadium catalyst having a pore size distribution with a mean pore diameter of at least 230 A. The molybdenum / vanadium catalyst was prepared in the following manner. The alumina was prepared by the method described in Example 1, impregnated with a molybdenum / vanadium impregnation solution prepared as follows. A first solution was developed by the combination of 2.14 grams of (NH4) 2Mo207, 3.21 grams of Mo03, 0.56 grams of 30% (hydrogen peroxide) H202, 0.14 grams of monoethanolamine (MEA), and 3.28 grams of deionized water to form a suspension. The suspension was heated to 65 ° C until the solids dissolved. The heated solution was cooled to room temperature. A second solution was developed combining 3.57 grams of VOS04 with 40 grams of deionized water. The first and second solutions were combined and sufficient deionized water was added to bring the combined solution up to the volume of up to 82 ml to yield the molybdenum / vanadium impregnation solution. The alumina base was impregnated with the vanadium / molybdenum impregnation solution, allowed to stand for 2 hours with occasional stirring, dried at 125 ° C for several hours, and calcined at 480 ° C for 2 hours. The resulting catalyst contained, per gram of catalyst, 0.02 grams of vanadium and 0.02 grams of molybdenum, with the balance being the base. The molybdenum / vanadium catalyst with one has a pore size distribution with an average pore diameter of 300 A. This example demonstrates the preparation of a metal catalyst from column 6 and metal from column 5 having a pore size distribution with a mean pore diameter of at least 230 A. Example 5. Contact of a crude feed with three catalysts. A tubular reactor was equipped with a centrally located hot water tank with thermocouplers to measure temperatures through the catalyst bed. The catalyst bed is formed by filling the space between the hot water tank and the inner wall of the reactor with catalysts and silicon carbide (20 mesh, Stanford Materials; Aliso Viejo, CA). It is believed that under the process conditions described herein such silicon carbide has low catalytic properties, if any. All the catalysts were mixed with an equal volume amount of silicon carbide before placing the mixture in the portions of the reactor contact zone. The flow of crude feed to the reactor was from the top of the reactor to the bottom of the reactor. Silicon carbide was placed in the lower part of the reactor to serve as a lower base. A mixture of catalyst / lower silicon carbide (42 cm3) was placed in the upper part of the silicon carbide to form a lower contact zone. The lower catalyst has a pore size distribution with an average pore diameter of 77 A, with 66.7% of the total number of pores in the pore size distribution having a pore diameter of 20 A of the average pore diameter. The lower catalyst has 0.095 grams of molybdenum and 0.025 grams of nickel per gram of catalyst, with the balance being the base of alumina. A mixture of medium catalyst / silicon carbide (56 cm 3) was placed above the lower contact zone to form a medium contact zone. The average catalyst has a pore size distribution with an average pore diameter of 98 A, with 66.7% of the total number of pores in the pore size distribution having a pore diameter of 24 A of the average pore diameter. The middle catalyst contained 0.02 grams of nickel and 0.08 grams of molybdenum per gram of catalyst, with the balance being the base of alumina. An upper catalyst / silicon carbide (42 cm 3) mixture was placed above the middle contact zone to form a superior contact zone. The upper catalyst has a pore size distribution with an average pore diameter of 192 A and contained 0.04 grams of molybdenum per gram of catalyst, with the balance being primarily the base range of alumina. Silicon carbide was placed above the upper contact zone to fill the dead space and to serve as a preheating zone. The catalyst bed was charged in a Lindberg furnace which includes five heating zones corresponding to the preheating zone, the upper, middle and lower contact zones and the lower base. The catalysts were sulphided by introducing a gaseous mixture of 5 vol% hydrogen sulfide and 95 vol% hydrogen gas in the contact zones at a rate of 1.5 liters of gas mixture per volume (ml) of total catalyst (silicon carbide not it is' counted as part of the catalyst volume). The temperatures of the contact zone were increased to 204 ° C (400 ° F) for 1 hour and set at 204 ° C for 2 hours. After holding the temperature at 204 ° C, the contact zones were extensively expanded to 316 ° C (600 ° F) at a rate of 10 ° C (50 ° F) per hour. The contact zones were maintained at 316 ° C for one hour, then they were extensively raised to 370 ° C (700 ° F) for 1 hour and held at 370 ° C for two hours. The contact zones were allowed to cool to room temperature. Crude was leaked from the Mars platform in the Gulf of Mexico, then heated in a furnace at a temperature of 93 ° C (200 ° F) for 12 to 24 hours to form the crude feed having the properties summarized in the Table 1, figure 7. The crude feed is poured to the upper part of the reactor. The crude feed flows through the preheating zone, the upper, middle and lower contact zone and the lower base of the reactor. The crude feed was contacted with each of the catalysts in the presence of hydrogen gas. The contact conditions were as follows: the rate of hydrogen gas and feed of crude supplied to the reactor was 328 Nm3 / m3 (2000 SCFB), LHSV was 1 h "1, and pressure was 6.9 MPa (1014.7 psi). The three contact zones were heated to 370 ° C (700 ° F) and maintained at 370 ° C for 500 hours, then the temperature of the three contact zones was increased, staying in the following sequence: 379 ° C (715 ° F) for 500 hours, and then 388 ° C (730 ° F) for 500 hours, then 390 ° C (734 ° F) for 1800 hours, and then 394 ° C (742 ° F) for 2400 hours. The total product (ie, the crude product and the gas) leaves the catalyst bed. The total product was introduced into the liquid gas phase separator. In the liquid gas separator, the total product was separated into crude product and gas. The gas inlet to the system was measured with a mass flow controller. The gas leaving the system is measured with a wet test meter. The crude product is periodically analyzed to determine the percentage by weight of the components of the crude product. The averaged results of the determined weight percentages of the components are listed. Table 1 of Figure 7 summarizes the properties of the crude product.

As shown in Table 1, the crude product has a sulfur content of 0.0075 grams, a residue content of 0.255 grams, and an oxygen content of 0.0007 grams per gram of crude product. The raw product has an MCR content rate and C5 asphaltene content of 1.9 and a TAN index of 0.09. The total nickel and vanadium is 22.4 tpp. The useful life of the catalysts was determined by measuring the temperature of the heavy average bed (for its acronym in English "WABT") versus the length of execution of the crude feed. The useful life of the catalysts can be correlated to the temperature of the catalyst bed. It is believed that as the useful life of the catalyst decreases WABT increases. Figure 8 is a graphic representation of WABT versus time ("t") for the improvement of the crude feed in the contact zones described in this example. Curve 136 represents the average WABT of the three contact zones versus the runtime hours for contact of a crude feed with the upper, middle and lower catalysts. During most of the execution time, the WABT of the contact zones changed only by approximately 20 ° C. From the relatively stable WABT, it was possible to estimate that the catalytic activity of the catalyst has not been affected. Generally, 3000-3500 hours of pilot unit execution time is correlated to 1 year of commercial operation. This example demonstrates that contacting the crude feed with a catalyst having a pore size distribution with an average pore diameter of at least 180 Á and with additional catalysts having a pore size distribution with a pore diameter medium of between 90-180 A, with at least 60% of the total number of pores in the pore size distribution having a pore diameter of 45 A of the average pore diameter, with controlled contact conditions, produced a total product which includes the crude product. As measured by the P value, the stability of the total product / crude feed mixture is maintained. The crude product has the reduced TAN index, reduced Ni / V / Fe content, reduced sulfur content, and reduced oxygen content relative to the crude feed, while the residue content and the VGO content of the crude product were of 90% -110% of the properties of the crude feed.

Example 6. Contact of a crude feed with two catalysts having a pore size distribution with a mean pore diameter in the range of 90-180 Á. The reactor apparatus (except for the number and content of the contact zones), the catalyst sulfurization method, the total product separation method and the crude product analysis method were the same as those described in Example 5. Each The catalyst is mixed with an equal volume of silicon carbide. The crude feed flow was from the reactor from the top of the reactor to the bottom of the reactor. From the bottom to the top, the reactor was filled in the following manner. Silicon carbide was placed at the bottom of the reactor to serve as the bottom base. A mixture of silicon carbide / lower catalyst (80 cm3) is placed on the silicon carbide to form a lower contact zone. The lower catalyst has a pore size distribution with an average pore diameter of 127 A, with 66.7% of the total number of pores in the pore size distribution having a pore diameter of 32 A of the average pore diameter. The lower catalyst includes 0.11 grams of molybdenum and 0.02 grams of nickel per gram of catalyst, with the balance being the base. The silicon carbide / top catalyst mixture (80 cm 3) was placed above the contact zone to form the upper contact zone. The upper catalyst has a pore size distribution with an average pore diameter of 100 A, with 66.7% of the total number of pores in the pore size distribution having a pore diameter of 20 A of the average pore diameter. The lower catalyst includes 0.03 grams of nickel and 0.12 grams of molybdenum per gram of catalyst, with the balance being alumina. Silicon carbide is placed over the first contact zone to fill the dead space and to serve as a preheating zone. The catalyst bed was loaded in a; Lindberg furnace that includes four heating zones corresponding to the • preheating zone, the two contact zones and the lower base. It was poured over the top of the BS-4 crude reactor (Venezuela) which has the properties summarized in Table 2, figure 9. The crude feed flows through the preheat zone, the upper and lower contact zone and the lower base of the reactor. The crude feed was contacted with each of the catalysts in the presence of hydrogen gas. The contact conditions were as follows: the rate of hydrogen gas for the crude feed providing the reactor was 160 Nm3 / m3 (1000 SCFB), LHSV was 1 hf1, and pressure was 6.9 MPa (1014.7 psi). The two contact zones were heated to 260 ° C (500 ° F) and maintained at 260 ° C for 287 hours. Then the temperature of the two contact zones was increased, staying in the following sequence: 270 ° C (525 ° F) for 190 hours, then 288 ° C (550 ° F) for 216 hours, then 315 ° C (600 ° C) F) for 360 hours, and then 343 ° C (650 ° F) for 120 hours for a total execution time of 1173 hours. The total product leaves the reactor and separates as described in Example 5. The crude product has an average TAN index of 0.42 and an average API gravity of 12.5 during processing. The crude product has 0.0023 grams of sulfur, 0.0034 grams of oxygen, 0.441 grams of VGO and 0.378 grams of waste per gram of raw product. In Table 2 in Figure 9, additional properties of the crude product are presented. This example demonstrates that the contact of the crude feed with the catalysts having pore size distributions with a mean pore diameter in the range of 90 to 180 A, produced a crude product having a reduced TAN index, content of Ni / V / Fe reduced, and a reduced oxygen content, relative to the properties of the crude feed, while the residue content and the VGO content of the crude product was 99% and 100% of the respective properties of the crude feed.

Example 7. Contact of the crude feed with two catalysts. The reactor apparatus (except the number and content of the contact zones), the catalysts, total product separation method, crude product analysis, and catalyst sulfurization method were the same as described in Example 6. It was poured above the top of the reactor, a crude source (crude BC-10) having the properties summarized in Table 3, figure 10. The crude feed flows through the preheating zone, upper contact zone and lower and the lower base of the reactor. The contact conditions were as follows: the rate of hydrogen gas to the crude feed supplied to the reactor was 80 Nm3 / m3 (500 SCFB), LHSV was 2 h "1, and pressure was 6.9 MPa (1014.7 psi). The two contact zones were extensively heated to 343 ° C (650 ° F). The total execution time was 1007 hours. The raw product has an average TAN index of 0.16 and an average API severity of 16.2 during processing. The crude product has 1.9 tppm of calcium, 6 wtppm of sodium, 0.6 wtppm of zinc, and 3 wtppm of potassium. The crude product has 0.003 3 grams of sulfur, 0.002 grams of oxygen, 0.376 grams of VGO and 0.40 1 grams of waste, per gram of crude product. In Table 3 in Figure 10. This example demonstrates that the contact of the crude feed with selected catalysts with pore size distributions in the range of 90-180 A, produces a crude product having a low TAN index, total of reduced calcium, sodium, zinc, and potassium content, while the sulfur content, VGO content, residue content of the crude product was 76%, 94%, and 103% of the respective properties of the crude feed.

Examples 8 to 11. Contact of a crude feed with four catalyst systems at various contact conditions. Each reactor apparatus (except the number and content of the contact zones), each catalyst sulfurization method, each total product separation method, and each product crude analysis were the same as those described in Example 5. mix all the catalysts with silicon carbide at a volume rate of 2 parts of silicon carbide per 1 part of catalyst unless otherwise indicated. The flow of crude feed through each of the reactors was from the top of the reactor to the bottom of the reactor. Silicon carbide was placed in the lower part of the reactor to serve as a lower base. Each reactor has a lower contact zone and a superior contact zone. After placing the silicon carbide / catalyst mixtures in the contact zones of each reactor, silicon carbide was placed on top of the contact zone to fill the dead space and to serve as a preheating zone in each reactor. Each reactor was charged in a Lindberg furnace including four heating zones corresponding to the preheating zone, the two contact zones and the lower base. In example 8, a mixture of molybdenum / nickel catalyst / uncalcined silicon carbide (48 cm3) was placed in the lower contact zone. The catalyst includes, 0.146 grams of molybdenum, 0.047 grams of nickel, and 0.021 grams of phosphorus, per gram of catalyst, with the balance being the alumina base. The mixture of silicon carbide / molybdenum catalyst (12 cm3) with the catalyst having a pore size distribution with an average pore diameter of 180 A was placed in the upper contact zone. The molybdenum catalyst has a total content of 0.04 grams of molybdenum per gram of catalyst, with the balance being the base that includes at least 0.50 grams of alumina range per gram of base. In Example 9, the mixture of silicon carbide / uncalcined cobalt / molybdenum catalyst (48 cm3) was placed in both contact zones. The uncalcined cobalt / molybdenum catalyst includes 0.143 grams of molybdenum, 0.043 grams of cobalt, and 0.021 grams of phosphorus with the balance that is the base of alumina. The mixture of molybdenum catalyst / silicon carbide (12 cm 3) was placed in the upper contact zone. The molybdenum catalyst was the same as in the upper contact zone of Example 8. In Example 10, the molybdenum catalyst is mixed as described in the upper contact zone of Example 8 with silicon carbide and placed in both zones of contact (60 cm3). In example 11, a mixture of uncalcined molybdenum / nickel catalyst / silicon carbide (48 cm3) was placed in the bottom of the contact zone. The uncalcined nickel / molybdenum catalyst includes, 0.09 grams of molybdenum, 0.025 grams of nickel, and 0.01 grams of phosphorus per gram of catalyst, with the balance being the base of alumina. The mixture of molybdenum catalyst / silicon carbide (12 cm 3) was placed in the upper contact zone. The molybdenum catalyst was the same as in the upper contact zone of Example 8. Crude was leaked from the Mars platform (Gulf of California).

Mexico), then heated in an oven at room temperature 93 ° C (200 ° F) for 12-24 hours to form the crude feed of Examples 8-11 having the properties summarized in Table 4, Figure 11. The crude feed was poured on top of the reactor in these examples. The crude feed flows through the preheating zone, the upper and lower contact zone and the bottom-bottom of the reactor. The crude feed was contacted with each of the catalysts in the presence of hydrogen gas. For each example the contact conditions were as follows: the rate of hydrogen gas and crude feed during contact was 160 Nm3 / m3 (1000 SCFB), and the total pressure of each system was 6.9 MPa (1014.7 psi) . The LHSV was 1.0 h "1 during the first 200 hours of contact, and then it was decreased to 1.0 h_1 for the remaining contact time, the temperatures in all contact zones were 343 ° C (650 ° F) for 500 contact hours After 500 hours, the temperature in all the contact zones was controlled as follows: the temperature in the contact zones rose to 354 ° C (670 ° F), it was held at 354 ° C during 200 hours, rose to 366 ° C (690 ° F), held at 366 ° C for 200 hours, rose to 371 ° C (700 ° F), held at 371 ° C for 1000 hours, rose to 385 ° C (725 ° C), it was held at 385 ° C for 200 hours, then it was raised to a final temperature of 399 ° C (750 ° C) and held at 399 ° C for 200 hours, for a time of Total contact time of 2300 hours Crude products were analyzed periodically to determine TAN index, hydrogen uptake by crude feed, P value, VGO content, content of residue and oxygen content. The average values of the properties of the raw products produced in Examples 8-10 are listed in Table 5 in Figure 11. Figure 12 is a graphical representation of the P value of the crude product ("P") versus time of execution ("t") for each of the catalyst systems of Examples 8-11. The crude feed has a P value of at least 1.5. The curves 140, 142, 144, and 146 represent the P value of the crude product obtained by contacting the crude feed with four catalyst systems of Examples 8-11 respectively. For 2300 hours, the P value of the remaining crude product was at least 1.5 for the catalyst systems of Examples 8-10. In example 11, the P value was above 1.5 for most of the execution time. At the end of the execution (2300 hours) of Example 11, the value of P was 1.4. From the P value of the raw product for each experiment, it can be deduced that the crude feed in each experiment remains relatively stable during the contact (for example, the crude feed is not separated by phases). As shown in Figure 12, the P value of the crude product remained relatively constant during the important portions of each experiment, except in Example 10, in which the P value increases. Figure 13 is a graphic representation of the uptake of net hydrogen by the crude sources ("H2") versus the execution time ("t") for four catalyst systems in the presence of hydrogen gas. Curves 148, 150, 152, 154 represent the net hydrogen uptake obtained by contacting the crude feed with each of the 8-11 catalyst systems, respectively. The net hydrogen uptake by the crude feed for an execution time of 2300 hours was in a range of between 7 and 48 Nm3 / m3 (43.8-300 SCFB). As shown in Figure 13, the net hydrogen uptake of the crude feed was relatively constant during each experiment. Figure 14 is a graphical representation of the residue content expressed as a percentage by weight of crude product ("R") versus run time ("t") for each of the catalyst systems of Examples 8-11. In each of the four experiments, the raw product has a residual content of 88-90% of the residue content of the crude feed. The curves 156, 158, 160, and 162 represent the residue content of the crude product obtained by contacting the crude feed with the catalyst systems of Examples 8-11, respectively. As shown in Figure 14, the residual content of the crude product remains relatively constant during significant portions of each experiment. Figure 15 is a graphical representation of the change in API gravity of the crude product ("? API") versus execution time ("t") for each of the catalyst systems in Examples 8-11. The curves 164, 166, 168, and 170 represent the API gravity of the crude product obtained by contacting the crude feed with the catalyst systems of Examples 8-11, respectively. In each of the four experiments, each raw product has a viscosity in the range of 58.3-72.7 cSt. The API gravity of each crude product increased by 1.5 to 4.1 degrees. The increased API gravity corresponds to an API gravity of the crude product in a range of 21.7 to 22.95. The API gravity in this range is 110-117% of the API gravity of the crude feed. Figure 16 is a graphical representation of the oxygen content, expressed as a percentage by weight, of the crude product ("02") versus the execution time ("t") for each of the catalyst systems of Examples 8-11. The curves 172, 174, 176, and 178 represent the oxygen content of the crude product obtained by contacting the crude feed with the catalyst systems of Examples 8-11, respectively. Each raw product has an oxygen content of maximum 16% of the crude feed. Each raw product has an oxygen content in the range of 0.0014-0.0015 grams, per gram of crude product during each experiment. As shown in FIG. 16, the oxygen content of the crude product remains relatively constant after a contact time of 200 hours. The relatively constant oxygen content of the crude product demonstrates that the selected organic oxygen compounds decrease during contact. Since the TAN index is also reduced in these examples, it can be deduced that at least a portion of the carboxylic-containing organic oxygen compounds selectively reduce with respect to the non-carboxylic organic oxygen compounds. In example 11, under reaction conditions of: 371 ° C (700 ° F), pressure of 6.9 MPa (1014.7 psi), and the rate of hydrogen with the crude feed of 160 Nm3 / m3 (1000 SCFB), the MCR content in the crude feed was reduced by 17.5% by weight, based on the weight of the crude feed. At 399 ° C (750 ° F) temperature, at the same pressure, and at the same rate of hydrogen with the crude feed, the MCR content in the crude feed was reduced by 25.4% by weight, based on the weight of the crude feed. In example 9, at reaction conditions of: 371 ° C (700 ° F), pressure of 6.9 MPa (1014.7 psi), and hydrogen rate with crude feed of 160 Nm3 / m3 (1000 SCFB), the content MCR in crude feed reduced to 17.5% by weight, based on the weight of the crude feed. At temperatures of 399 ° C (750 ° F), and at the same pressure, and the same rate of hydrogen and crude feed, the MCR content in the crude feed was 19% by weight, based on the weight of the crude feed. This increased reduction of the MCR content in the crude feed shows that the uncharged column 6 and 10 metal catalysts facilitate the reduction of the MCR content at higher temperatures than the non-calcined column 6 and 9 metal catalysts. These examples show that contact of a crude feed with a relatively high TAN index (TAN of 0.8) with one or more catalysts produces a crude product, while maintaining the stability of the total product / crude feed mix with a relatively small net hydrogen uptake. The raw product properties selected were of maximum 70% of the same properties of the crude feed, while the selected properties of the crude product were 20 to 30% of the same properties of the crude feed. Specifically, as shown in Table 4, each of the crude products was produced with a net hydrogen uptake by crude sources of maximum 44 Nm3 / m3 (275 SCFB). Such products have an average of T7? N of maximum 4% of the crude feed, and an average total Ni / V content of maximum 61% of the total Ni / V content of the crude feed, while maintaining a P value for, the crude feed above 3. The average residue content for each crude product was 88-90% of the residue content of the crude feed. The average VGO content for each crude product was 115-117% of the VGO content of the crude feed. The average API gravity of each crude product was 110-117% of the API gravity of the crude feed, while the viscosity of each crude product was a maximum of 45% of the viscosity of the crude feed.

Examples 12-14: Contact of a crude feed with catalysts having a pore size distribution with a mean pore diameter of at least 180 A with minimum hydrogen consumption. In Examples 12-14, each reactor apparatus (except for the number and content of the contact zones), each catalyst sulfurization method, each total product separation method and each raw product analysis were the same as those described in Example 5. All the catalysts are mixed with an equal volume of silicon carbide. The flow of crude feed to each reactor was from the top of the reactor to the bottom of the reactor. Silicon carbide was placed in the lower part of each reactor to serve as a lower base. Each reactor contained a contact zone. After placing the silicon carbide / catalyst mixtures in the contact zone of each reactor, silicon carbide is placed in the upper contact zone to fill the dead space and serve as a preheating zone in each reactor. Each reactor was charged in a Lindberg furnace which includes three heating zones corresponding to the preheating zone, the contact zone, and the bottom base. The crude feed was contacted with each of the catalysts in the presence of hydrogen gas. A mixture of silicon carbide / catalyst (40 cm.sup.3) was placed on silicon carbide to form the contact zone. For example 12, the catalyst is vanadium catalyst prepared as in Example 2. For Example 13, the catalyst was the molybdenum catalyst prepared as in Example 3. For example 14, the catalyst was the molybdenum / vanadium catalyst as prepared in example 4. The contact conditions for examples 12-14 were as follows: the rate of hydrogen and crude feed supplied to the reactor was 160 Nm3 / m3 (1000 SCFB), LHSV was 1 h "1, and the pressure was 6.9 MPa (1014.7 psi). The contact zones were heated extensively to 343 ° C (650 ° F) for a period of time and were maintained at 343 ° C for 120 hours for a period of Total execution of 360 hours The total products leave the contact zone and separate as described in example 5. The uptake of net hydrogen during contact was determined for each catalyst system In Example 12, the uptake of hydrogen net was -10.7 Nm3 / m3 (-6 5 SCFB), and the crude product has a TAN index of 6.75. In example 13, the net hydrogen uptake was 2.2-3.0 Nm3 / m3 (13.9-18.7 SCFB), and the crude product has a TAN index in the range of 0.3-0.5. In example 14, during contact of the crude feed with the molybdenum / vanadium catalyst the net hydrogen uptake was in the range of -0.05 Nm3 / m3 to 0.6 Nm3 / m3 (-0.36 SCFB to 4.0 SCFB), and the crude product has a TAN index of 0.2-0.5. From the net hydrogen uptake values during contact, it was estimated that hydrogen was generated at a rate of 10.7 Nm3 / m3 (65 SCFB) during contact of the crude feed and the vanadium catalyst. Hydrogen production during contact allows to use less hydrogen in the process relative to the amount of hydrogen that is used in conventional processes to improve the properties of disadvantageous crudes. The requirement of less hydrogen during contact tends to decrease the costs of crude processing. In addition, the contact of the crude feed with the molybdenum / vanadium catalyst produces a crude product with a TAN index that was lower than the TAN index of the crude product produced from the molybdenum catalyst individually.

Examples 15-18. Contact of the crude feed with a vanadium catalyst and an additional catalyst. Each reactor apparatus (except the number and content of the contact zones), each method of sulfurization of the catalyst, each method of separation of the total product, and each analysis of the crude product were the same as those described in Example 5. All the catalysts are mixed with silicon carbide at a volume rate of 2 parts of silicon carbide per 1 part of catalyst, unless otherwise indicated. The flow of crude feed to each reactor was from the top of the reactor to the bottom of the reactor. The silicon carbide was placed in the lower part of each reactor to serve as a lower base. Each reactor has one - lower contact area, and a superior contact area. After placing the silicon carbide / catalyst mixtures in the contact zones of each reactor, silicon carbide is placed on the upper contact zone to fill the dead space and to serve as a preheating zone in each reactor. Each reactor was charged in a Lindberg furnace which includes four heating zones corresponding to the preheating zone, two contact zones and the lower base. In each example, the vanadium catalyst is prepared as described in Example 2 and used with an additional catalyst. In example 15, another mixture of silicon carbide / additional catalyst (45 cm3) is placed in the lower contact zone, with another catalyst which is the molybdenum catalyst prepared by the method described in Example 3. The carbide mixture Silicon / vanadium catalyst (15 cm3) is placed in the upper contact zone. In example 16, a mixture of silicon carbide / other catalyst (30 cm3) is placed in the lower contact zone, with another catalyst which is a molybdenum catalyst prepared by the method described in Example 3. The carbide mixture Silicon / vanadium catalyst (30 cm3) is placed in the upper contact zone. In example 17, a mixture of another catalyst / silicone (30 cm3) is placed in the lower contact zone, with another catalyst which is a molybdenum / vanadium catalyst such as that which is prepared in Example 4. The catalyst mixture vanadium / silicon carbide (30 cm3) was placed in the upper contact zone. In Example 18, Pyrex® glass beads (30 cm 3) (Glass Works Corporation, New York, U.S.A.) are placed in each contact zone. It is poured into the upper part of the crude reactor (Santos Basin, Brazil) for Examples 15-18, which has properties that are summarized in Table 5, Figure 17. The crude feed flows through the preheating zone, the upper and lower contact zone, and the lower base of the reactor. The crude source is contacted with each of the catalysts in the presence of hydrogen gas. The contact conditions for each example were as follows: the rate of hydrogen gas and feed of crude supplied to the reactor was 160 Nm3 / m3 (1000 SCFB) during the first 86 hours and 80 Nm3 / m3 (500 SCFB) during the Remaining period of time, LHSV was 1 bf1 and the pressure was 6.9 MPa (1014.7 psi). The contact zones were extensively heated to 343 ° C (650 ° F) for a period of time and were maintained at 343 ° C for a total run time of 1400 hours. These examples demonstrate that the contact of the crude feed with a metal catalyst of column 5 having a pore size distribution with an average pore diameter of 350 A in combination with another catalyst having a pore size distribution with an average pore diameter in the range of 250-300 A, in the presence of a source of hydrogen, it produces a crude product with properties that change relative to the same properties of the crude feed, while the other properties of the feed of crude oil change only in relative small quantities with the same properties of crude oil. In addition, during processing, relatively little hydrogen uptake is observed from the crude feed. Specifically, as shown in Table 5, Figure 17, the crude product has a TAN index of maximum 15% of the TAN index of the crude feed for the examples Example 15-17. The crude product produced in examples 15-17 each have a total content of Ni / V / Fe of maximum 44%, an oxygen content of maximum 50%, and viscosity of maximum 75% relative to the same properties of the feed of crude. In addition, the raw products produced in the examples Example 15-17, each have an API gravity of 100-103% of the API gravity of the crude feed. In contrast, the crude product produced under non-catalytic conditions (Example 18), produces a product with increased viscosity and reduced API gravity relative to viscosity and API gravity of the crude feed. From the increased viscosity and reduced API gravity it may be possible to deduce that the coke formation and / or polymerization of the crude feed began.

Example 19. Contact of a crude feed to various LHSV. The contact systems and the catalysts are the same as those described in Example 6. The properties of the crude feeds are listed in Table 6, Figure 18. The contact conditions are as follows: the rate of hydrogen gas and crude feed provided "to the reactor was 160 Nm3 / m3 (1000 SCFB), pressure was 6.9 MPa (1014.7 psi), temperature in the contact zone was 371 ° C (700 ° F) throughout the run time In example 19, the LHSV during the contact increased in a period of time from 1 h-1 to 12 h-1, remained at 12 hf 1 for 48 hours, and then the LHSV was increased to 20. 7 h_1 and kept at 20.7 h "1 for 96 hours In Example 19, the crude product was analyzed to determine the TAN index, viscosity, density, VGO content, residue content, heteroatom content, and the content of metals in metallic salts of organic acids during the period of time when LHSV was at 12 h-1 and at 20.7 hf1.The average values of the properties of the raw products are shown in Table 6, Figure 18. As shown in Table 6, Figure 18, the raw product of Examples 19, has reduced TAN index and reduced viscosity relative to the TAN index and to the viscosity of the crude feed, while the API gravity of the crude product was 104-110% of the gravity API of the crude feed The weight ratio of the MCR content versus the C5 asphaltene content was at least 1.5 The sum of the MCR content and the C5 asphaltene content was reduced relative to the sum of the MCR content and of as pillars C5 of the crude feed. From the weight ratio of the MCR and asphaltenes C5 content and the reduced sum of the MCR and asphaltenes C5 content, it is deduced that the asphaltenes are decreased and not the components that tend to form coke. The crude product also has a total content of potassium, sodium, zinc, and calcium of maximum 60% of the total content of the same total metals of the crude feed. The sulfur content of the crude product was 80-90% of the sulfur content of the crude feed. Examples 6 and 9 show that the contact conditions can be controlled in such a way that the LHSV through the contact zone is greater than 10 bf1, comparing with the process with a LHSV of 1 hf1, to produce raw products with properties Similar. The ability to selectively change a property of a crude feed at liquid speeds for hours greater than 10 hf1 allows the contact process to be carried out in containers of relatively small size with commercially available containers. A smaller container allows the treatment of disadvantageous crudes to be carried out in production sites that have size restrictions (for example, in offshore installations).

Example 20. Contact of a crude feed at various contact temperatures. The contact systems and catalysts were the same as described in Example 6. The crude feed having the properties listed in Table 7 in Figure 19 was added to the top of the reactor and contacted with two. catalysts in two contact zones in the presence of hydrogen to produce crude product. The two contact zones were operated at different temperatures. Contact conditions in the upper contact area were as follows: LHSV of 1 hf1; the temperature in the upper contact zone was 260 ° C (500 ° F); the rate of hydrogen and crude feed was 160 Nm3 / m3 (1000 SCFB); and pressure was 6.9 MPa (1014.7 psi). The contact conditions in the lower contact area were as follows: the LHSV was 1 h-1; the temperature in the lower contact zone was 315 ° C (600 ° F); rate . of hydrogen and crude feed was 160 Nm3 / m3 (1000 SCFB); and pressure was 6.9 MPa (1014.7 psi). The total product leaves the lower contact zone and is introduced into a liquid gas phase separator. In the liquid gas phase separator, the total product was separated into raw product and gas. The crude product was periodically analyzed to determine the TAN index and the C5 asphaltene content. The average values of the properties of the crude product obtained during execution are listed in Table 7, Figure 19. The crude feed has a TAN index of 9.3 and a content of C5 asfltenos of 0.055 grams of C5 asphaltenes per gram of feed of crude. The raw product has an average TAN index of 0.7 and an average C5 asphaltene content of 0.039 grams of C5 asphaltenes per gram of raw product. The content of asphaltenes Cs of the crude product was of maximum 71% of the content of asphaltenes Cs of the raw product. The total content of potassium and sodium in the crude product was of maximum 53% of the total content of the same metals in the crude feed. The TAN index of the crude product was of maximum 10% of the TAN index of the crude oil supply. A P value of 1.5 or more was maintained during the contact. As shown in Examples 6 and 20, they have a first contact temperature (in this case, higher) of 50 ° C lower than the contact temperature of the second zone (in this case, lower) which tends to improve the reduction of the content of asphaltenes Cs in the crude product in relation to the content of asphaltenes C5 of the crude feed. In addition, the reduction of metal content in metal salts of organic acids is improved by using controlled temperature differentials. For example, the reduction of the total sodium and potassium content of the crude product of Example 20 is improved relative to the reduction of the total potassium and sodium content of the crude product of Example 6 with stability of the total product / crude feed mix. relatively constant for each example, as measured by the P value. Using a lower temperature in the first contact zone, it allows to remove the components with high molecular weight (for example, asphaltenes C5 and / or metallic salts of organic acids) that have tendency to form polymers and / or compounds having physical properties of softness and adhesiveness (for example gums or tars). The elimination of these compounds at lower temperatures allows such compounds to be removed before connecting and coating the catalysts, which increases the life of those that operate at higher temperatures and which are located after the first contact zone.

Example 21. Contact of crude feed and catalyst in suspension form. A crude metal catalyst and / or an application catalyst (0.0001-5 grams or 0.02-4 grams of catalyst per 100 grams of crude feed) may, in some embodiments, be subjected to suspension with crude feed and react under the following conditions: temperature in the range of 85-425 ° C (185-797 ° F), pressure in the range of 0.5-10 MPa, and ratio of hydrogen source and crude feed of 16-1600 Nm3 / m3 for a period of time. After a sufficient reaction time to produce a crude product, it is separated from the catalyst and / or residual crude feed using a separation apparatus, such as a filter and / or centrifuge. The crude product may have a TAN index, changed iron, nickel, and / or vanadium content and a reduced Cs asphaltene content relative to the crude feed. Other modifications and alternative embodiments of various aspects of the invention will be apparent to those skilled in the art in view of this description. Accordingly, this description should be considered as illustrative only and is for the teaching purposes of those skilled in the art in the general manner of carrying out this invention. It should be understood that the forms of the invention shown and described herein, should be taken as examples of modalities. The elements and materials to be replaced by those illustrated and described herein, the parts and processes may be reversed and certain features of the invention may be used independently, as would be clear to the person skilled in the art after having the benefit of this description of the invention. Changes may be made to the elements described herein without departing from the spirit and scope of the invention as described in the following claims.

It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Claims

CLAIMS Having described the invention as above, the contents of the following claims are claimed as property: 1. Method for producing a crude product, characterized by comprising: contacting a crude feed with one or more catalysts to produce a total product that includes the crude product, where the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the crude feed has a total acid number (TAN) of at least 0.3, and at least one of the catalysts has a distribution of pore size with a mean pore diameter in the range of 90 A to 180 A, with at least 60% of the total number of pores in the pore size distribution having a pore diameter of 45 A pore diameter medium, wherein the pore size distribution is as determined by the ASTM method D4282; and controlling the contact conditions so that the crude product has a TAN index of maximum 90% of the TAN index of the crude feed, where the TAN index is as determined by the ASTM D664 method. Method according to claim 1, characterized in that the TAN index of the crude product is maximum 50%, 30%, or maximum 10% of the TAN index of the crude feed. Method according to claim 1, characterized in that the TAN index of the crude product is in the range of 1-80%, 20-70%, 30-60% or 40-50% of the TAN index of the crude feed . Method according to any of claims 1-3, characterized in that the TAN index of the crude product is in the range of 0.001 to 0.5, 0.01 to 0.2, or 0.05 to 0.1. Method according to any of claims 1-4, characterized in that the TAN index of the crude product is in the range from 0.3 to 20, 0.4 to 10, or from 0.5 to 5. 6. Method for producing a crude product, characterized in that it comprises: contacting the crude feed with one or more catalysts to produce a total product that includes the crude product, where it is a liquid mixture at 25 ° C and 0.101 MPa, the crude feed comprises one or more alkaline metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, the crude feed has a total content, per gram of crude feed, of one or more alkaline metal salts, of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or mixtures thereof, of at least 0.0000 1 grams, and at least one of the catalysts has a pore size distribution with a mean pore diameter of at least 90 Á at 180 Á, and at least 60% of the total number of pores in the pore size distribution having a pore diameter of 45 A of the pore diameter medium, wherein the pore size distribution is as determined by the ASTM method D4282; and control the contact conditions in such a way that the raw product has a total content of alkali metal, and so alkaline earth metal, in metallic salts of organic acids of maximum 90% of the content of alkali metal, and alkaline earth metal, in metal salts of acids Organic of the crude feed, wherein the content of alkali metal, and alkaline earth metal in metal salts of organic acids is determined is as determined by the method ASTM D1318. Method according to claim 6, characterized in that the total content of alkali metal, and alkaline earth metal, in metal salts of organic acids in the crude product is maximum 50%, 10%, or maximum 5% of the metal content alkaline, and alkaline earth metal, in metallic salts of organic acids in the crude feed. Method according to claim 6, characterized in that the total content of alkali metal, and alkaline earth metal, in metal salts of organic acids in the crude product is in the range of 1-80%, of 10-70%, 20-60% or 30-50% of the content of alkali metal, and alkaline earth metal, in metal salts of organic acids in the crude feed. 9. Method according to any of claims 6-8, characterized in that the crude product has from 0.0000001 to 0.00005 grams, from 0.0000003 to 0.00002 grams, or from 0.000001 to 0.00001 grams of alkali metal, and alkaline earth metal, in metallic salts of organic acids per gram of crude product. A method for producing a crude product, characterized in that it comprises: contacting a crude feed with one or more catalysts to produce a total product that includes the crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the crude feed has a total content of Ni / V / Fe per gram of at least 0.00002, and at least one of the catalysts has a pore size distribution with an average pore diameter of 90 A at 180 Á , with at least 60% of the total number of pores in the pore size distribution having a pore diameter of 45 A of the average pore diameter, wherein the pore size distribution is as determined by the ASTM method D4282; and controlling the contact conditions in such a way that the crude product has a total content of Ni / V / Fe of maximum 90% of the Ni / V / Fe content of the crude feed, where the content of Ni / V / Fe is as determined by the ASTM D5708 method. Method according to claim 10, characterized in that the content of Ni / V / Fe of the crude product is maximum 50%, 10%, 5% or maximum 3% of the Ni / V / Fe content of the feed of raw. Method according to claim 10, characterized in that the content of Ni / V / Fe of the crude product is in the range of 1-80%, 10-70%, 20-60% or 30-50% of the content of Ni / V / Fe of crude feed. Method according to any of claims 10-12, characterized in that the raw product has, per gram of crude product, from 0.0000001 grams to 0.00005 grams, from 0.0000005 grams to 0.00001 grams, or from 0.000001 grams to 0.000005 grams of content of Ni / V / Fe. 1 . Method according to any of claims 1-13, characterized in that the catalyst has the pore size distribution comprising one or more metals of columns 5 to 10 of the Periodic Table, one or more compounds of one or more metals of columns 5 to 10. and / or mixtures thereof. 15. Method according to claim 14, characterized in that the catalyst has the pore size distribution further comprising one or more elements of column 15 of the Periodic Table, and / or one or more compounds of one or more elements of column 15. 16. Method according to any of claims 1 to 15, characterized in that the pore diameter is 35 Á or 25 Á of the average pore diameter. Method according to any of claims 1 to 16, characterized in that one or more catalysts further comprise an additional catalyst, which has a pore size distribution with an average pore diameter of at least 60 A or at least 180 TO. 18. Method of compliance with the claim 17, characterized in that the contact comprises contacting the crude feed with the catalyst subsequent to the contact of the crude feed with the additional catalyst. 19. Method according to any of claims 1-18, characterized in that the crude feed is brought into contact in the contact zone that is in or coupled to an offshore installation. 20. Method according to any of claims 1-19, characterized in that the contact comprises contacting the presence of a source of hydrogen. 21. Method according to any of claims 1 to 20, characterized in that it additionally comprises the combination of crude product with a crude oil equal to or different from the crude feed to form a mixture. 22. Raw product, characterized in that it is obtained by a method according to any of claims 1 to 21. 23. Crude product, characterized in that it has, per gram of crude product: maximum 0.004 grams of oxygen, as determined by the method ASTM E385; maximum 0.003 grams of sulfur, as determined by ASTM method D4294; maximum 0.04 grams of basic nitrogen, as determined by ASTM method D2896; and at least 0.2 grams of residue, as determined by the ASTM D5307 method; and the crude product has a total acid number (TAN) of maximum 0.5, as determined by the ASTM D664 method. 24. Crude product according to claim 23, characterized in that the TAN index of the crude product is maximum 0.3 or maximum Oil. 25. Crude product according to claim 23 or 24, characterized in that the raw product also has, per gram of crude product, a total nitrogen content of at least 0.01 grams, as determined by the method ASTM D5762. 26. Crude product according to claims 23 to 25, characterized by that it also has per gram of crude product: at least 0.001 grams of hydrocarbons with a boiling range distribution of between 95 ° C and 260 ° C at 0.101 MPa , at least 0.001 grams of hydrocarbons with a boiling point range between 260 and 320 ° C at 0.101 MPa, at least 0.001 grams of hydrocarbons with a boiling point range of 320 ° C to 650 ° C at 0.101 MPa. 27. Crude product according to any of claims 23 to 26, characterized in that the raw product also has maximum 0.00005 grams of nickel and total vanadium, per gram of crude product, where the nickel and vanadium weights are as determined by the ASTM D5708 method. 28. Method for producing a transport fuel, combustion fuel, lubricant, or chemical compound, characterized in that it comprises processing a crude product or mixture according to any of claims 22 to 27. 29. Method according to claim 28, characterized in that the processing comprises distilling the crude product or mixture in one or more fractions of distillate. 30. Method according to claim 28 or 29, characterized in that the processing comprises hydrotreating.