TW200532010A - Systems, methods, and catalysts for producing a crude product - Google Patents

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 DEG 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

200532010 IX. Description of the invention: [Technical field to which the invention belongs] The present invention relates generally to systems, methods, and catalysts for processing crude oil feeds, and to the use of such systems, methods, and catalysts to produce compositions. More specifically, the specific examples described herein relate to systems, methods, and catalysts used to convert crude oil feeds to total products, where the total product contains raw / free products at 25 ° C and It is a liquid mixture at 0.1 MPa and has one or more changed properties compared to the individual properties of the crude feed. [Prior technology] em 刖 transportation, processing, and processing of crude oil of inappropriate quality are commonly referred to as "inferior crude oils" acid I two raw materials ", which may include the total acidity of the crude oil feed The value of "(TAN ,,)" is a knife. The relatively high τ processing & κN < < " > shell crude oil may cause W ^^^ rb ^ corrosion during the rotation and / or during the cutting of this grade 4 crude oil. Remove the acidic components from the crude oil. Or + This involves the neutralization of acidic compounds with various alkali chemistry, corrosion resistance, chemical resistance, and / or processing equipment. Corrosion usually involves a considerable amount of expense ^ Corrosion resistant metal y e i, which is used in current equipment is not what we expect. May involve another method for making rotten residues on ~ β / 々 夂 in round and / or processing inferior to inferior crude oil. The use of corrosion # ρ Μ ″ to add corrosion inhibitors and / or; ^ inhibitors may have a negative impact on the equipment used to process crude oil, the quality of the products manufactured / used-Bei Libei crude oil usually contains phase depletion Once the material is used, it will be far away. Such large amounts of residues are difficult to be rotated and / or directed. Τ expensive 200532010 atoms (such as sulfur, oxygen, and other harmful to the catalyst) Inferior crude oils often contain organically bound heteronitrogens. Organically bound heteroatoms can react in a number of situations. Inferior crudes may contain a significant amount of metal contaminants such as nickel, Syria, and / or iron. During processing of such crudes Metal pollutants and / or gold: Compounds of pollutants may be deposited on the catalyst surface or in the catalyst's pore volume. Such deposits may cause a decrease in catalyst activity. Coke may be processed during the processing of inferior crude oil Will form and / or deposit sharply on the catalyst surface. The cost of regenerating the catalytic activity of a catalyst contaminated with coke may be expensive. The high temperature used during regeneration may also cause the catalyst Reduced activity and / or cause catalyst degradation. Inferior crude oils may contain metals in the form of metal salts of organic acids (such as calcium, potassium di and / or sodium). Metals in the form of metal salts of organic acids typically cannot be treated by the method 'Such as desalination and / or pickling is separated from inferior crude oil. Β When organic metals in the form of metal salts of organic acids are present, the method often encounters the question "Compared with the conventional deposition of the catalyst near the surface of the catalyst, The metal in the form of an organic acid metal salt may be preferentially deposited in the pore volume between the catalyst particles, and the man, β ^ / 疋 is on the top of the catalyst bed. Contaminants, such as organic acids = a tragic 'metal deposit on the top of the catalyst bed will usually result in an increase in the μ pressure drop through contact and actual contact. Furthermore, metals in the metal salt state may cause rapid deactivation of the catalyst. Per gram inferior :: The oil may contain organic oxygen compounds. Problems may be encountered during processing facilities for processing inferior crude oils having an oxygen content of at least 0.002 grams of oxygen in crude oil with an oxygen content of f. During the processing of the organic oxygen compound in 200532010, it will be hot again. This will generate high-grade oxides (such as ketone and / or alcohol from alcohol and / or ether from acid), which is difficult to remove from processed crude oil. Remove and / or may corrode / contaminate equipment and block pipelines during processing. ^ / Mass crude oil may contain unsaturated hydrocarbons. When processing unsaturated hydrocarbons, in particular, if unsaturated flakes # produced by the cracking method are produced, the average amount of hydrogen must generally be increased. Hydrogenation during processing, which typically involves the use of active gasification catalysts, may inhibit the formation of coke by unsaturated fragments. Hydrogen is expensive to produce and / or expensive to transfer to processing equipment. Inferior crude oil also tends to show instability during processing with conventional equipment: qualitative. Crude oil instability tends to cause component phase separation and / or the formation of non-ideal by-products (such as chlorine sulfide, tritium, and carbon dioxide) during processing. Conventional methods are often lacking. The selected properties of high-quality crude oils, but not the ability to change other properties of low-quality crude oils. For example, it is often known that there is often a lack of significant reduction of TAN in low-quality crude oils while at the same time only the desired amount of energy: Several of the contents of ingredients (such as sulfur or metal contaminants) are used to improve the mouth of the crude oil. Mouth spoon method includes adding a diluent to the inferior: crude oil to reduce the weight percentage of the ingredients that cause adverse properties. Narrow: Adding a diluent is usually due to the cost of the diluent and / or the cost of the crude oil. The addition of diluent to inferior crude oil may reduce the stability of this oil under certain circumstances. Awarded to S ^ akar et al U.S. Patent No. 6,547,957; granted 200532010

6,277,269 by Meyers et al .; 6 plus 颁 by Ruyou et al. 5,928,502 by Bearden et al., 仏 by Ruding et al. By ⑽⑽ et al. # 5,897,769; by Trachte 5,871,636, and materials Tanaka # 5,85i, 38i describe various methods, systems and catalysts for processing crude oil. However, the methods, systems, and catalysts described in these patents have limited applicability due to many of the techniques proposed above. / 、 Among other things, inferior crude oil usually has non-ideal properties (for example, a relatively high TAN, a tendency to become Wei Xianghe ο during processing ′ and / or a tendency to eliminate leprosy during processing). Other non-ideal properties include a considerable amount of non-ideal components (such as residues, organically bound heteroatoms, metal contaminants, metals in the form of metal salts of organic acids' and / or organic oxygen compounds). This type of property tends to lead to problems with the knowledge of Lianxiang β / 4, Lianyi Baizhi's delivery and / or processing equipment, including

During the treatment, the number of rot insects increased, and the number of catalysts I9 and catalyst π0) 7 decreased, the process was blocked, and / or hydrogen increased ^. Therefore, there is still a significant economic need for reforming systems, methods, and / or catalysts to convert inferior crude oil into crude products with more desirable properties. There is also a significant economic and technical need for systems, systems, methods, and / or media that can change the selected properties of inferior crude oils and touch other properties of Mingbei crude oil. [Summary of the Invention] The production system of this month is related to a system and a catalyst for converting a crude oil feed into a crude product containing crude oil and in some specific examples a non-condensable gas. The present invention is also generally directed to compositions containing novel ',,' and & Such compositions can be obtained using the system described in this article and the 200532010 method. The present invention provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with one or more catalysts to produce a crude oil-containing product / wherein the crude oil product is in a liquid state below = the original: the feed has at least 0.3 # TAN, the at least one catalyst has a pore size distribution with a median pore position in the range of 9G A to 18G A 'The total number of pores in the pore size distribution has a pore size in the 45A median pore size range, where The distribution is determined by ASTM &2; and the contact conditions are controlled so that the crude oil product has a TAN of the crude oil feed with a TAN of up to 90%, where TAN is determined by ASTM method D664. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture under the condition of 0.1 Mpa and the crude oil; The feed has at least G 3 @ TAN, and the at least one catalyst has a pore size distribution with a median pore size of at least 90A, which is determined by ASTM & D428 ^^ j. It contains 0.1 to 0.08 grams of platinum,-or more compounds, or mixtures thereof; and controls the contact conditions so that the crude oil product has a TAN of TAN of up to 90% of the crude oil feed. Among them, TAN is measured by ASTM method D664. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at a temperature of 0,001 Mpa, The crude feed has a TAN of at least 0.3, as measured by asmd664, and the at least one catalyst has a pore size distribution with a median pore size of at least 18qA. 200532010 It is measured by ASTM4 D4282, and the catalyst has a cycle containing Table 1 shows the pore size distribution of one or more metals, 6 or more compounds of one or more metals of the Periodic Table, or a mixture thereof; and controls the contact conditions so that the crude oil product has a TAN of up to 4 90% of the crude oil into the TAN. , Where TAN is determined by ASTM method D664. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product: wherein the crude oil product is a liquid mixture under the conditions of G.1G1 Mpa, Now the feed has a TAN of at least 0.3, which is measured by ASTM method D664 twice to v. The catalyst contains: ⑷ one or more of the sixth column of the periodic table ^ belongs to the sixth column of the second periodic table—or Multi-metal—or multiple compounds,: ,,,,,,, and (b) one or more metals listed in Table 1 of the periodic table, one or more metals in Table 1—or multiple compounds, or a mixture thereof Mouthpieces, in which the molar ratio f of the total amount of metal in column 10 to the total amount of metal in column 6 f ... Within the range of, and control the contact conditions so that the crude oil product: there is at most 90% of the plutonium of the crude oil feed, wherein the tan series is determined by ASTM method D664. The invention also provides a method for producing a crude oil product, which comprises: contacting crude oil with one or more catalysts to produce a total product containing the crude oil product, = the crude oil product is a liquid mixture at 25 t and 0.101 MPa, and ^ Jinke has a TAN of at least 0.3. The one or more catalysts include: the first catalyst, which is contained in the first catalyst per gram, based on the weight of the metal, and contains 1 to 0.06 grams of The sixth or more metals of the periodic table, the sixth or more of the week, or one or more compounds of the metals, or a mixture thereof 10 200532010; and (b) the second catalyst, the second catalyst Among the two catalysts of the mother gram, 'the one or more metals containing at least 0,02 grams of column one of the periodic table', based on the weight of the catalyst, in the sixth column of the periodic table-or more metals-or more compounds, or Its mixture; and controlling the contact conditions so that the crude oil product exhibits a maximum of 90% of the crude oil feed, TAN of the crude oil, wherein TΛN is determined by ASTM method D664. The present invention also provides a catalyst composition comprising: (i) one or more metals in column 5 of the periodic table, one or more compounds of one or more metals in the periodic table, or a mixture thereof; (ii) a carrier, which has The content of osmium oxide is at least (M grams of θ oxide in the mother gram carrier, which is determined by X-ray diffraction: where the catalyst has a pore size distribution with a median pore size of at least 2%, and it is measured by ASTM method D4282 The present invention also provides a catalyst composition, which includes: (6) of the periodic table or more of the metal 'or 6 or more compounds of the periodic table' or a mixture of one or more of the metals' or a mixture thereof; The alumina content is at least ^ grams of θ oxidation | g per gram of carrier, which is determined by X-ray diffraction, where the catalyst has a pore size distribution with a median pore size of at least 23 ° A, which is determined by ASTM method D4282 The present invention also provides a catalyst composition, which includes: (a) the fifth or more metals of the periodic table, the five or more of the periodic table-one or more compounds of the plurality of metals, one of the six or more compounds of the periodic table Or more metals, gold of the sixth periodic table One or more compounds, or mixtures thereof; (b) containing Θ alumina having an alumina content of at least 0.1 g per gram of support, as determined by x-ray diffraction; wherein the catalyst has a median The pores with a pore diameter of up to 200532010 are less than 2 3 0 A. The fineness is determined by ASTM method D4282. 1 The present invention also provides a method for producing a catalyst, which includes: combining a carrier with—or a plurality of metals to Form a carrier ', θ oxidation, and one or more = "& substances, wherein the carrier contains ytterbium, / metal species including one or more mongolia of the fifth table of the periodic table, one of the fifth table of the periodic table < ^ &Amp;. One or more compounds, or "mixtures" of A metal species; heat treatment at least 4,000 ° C / degree τ heat treatment θ oxidation of the carrier / amp; and the formation of catalysts The catalyst has a pore size distribution with a median pore size of at least 230A, which is determined by the astm method 04282. The present invention also provides a method for producing a catalyst, which comprises: combining a carrier with one or more metals to form a carrier / Metal mixture, wherein the carrier contains Θ emulsified, and one or Kinds of metal include one or more metals in the sixth table of the periodic table, _ compounds of _ or more metals in the sixth table of the periodic table, or "daggers, ash heat treatment at a temperature of at least _C Θ oxidation | g support / Metal mixture 'and forming a catalyst, wherein the catalyst has a pore size distribution with a median pore size of at least 230 people, which is determined by the ASTM method 04282.

The present invention also provides a method for producing a crude oil product, comprising: contacting crude oil with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. (: And G.1G1 are purchased as a liquid mixture, the crude oil feed has at least 0.3 @ TAN, the at least one catalyst has a pore size distribution from median pores to v of 180A, which is measured by the method BUM The medium has a pore size distribution containing Θ oxide and one or more metals of the sixth table of the periodic table, one or more compounds of one or more metals of column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product TAN with a maximum of 90% of the crude oil feed, of which TAN 12 200532010 is determined by ASTM method D 6 64. ❿ The present invention also provides a method for producing crude oil products, which includes: in the presence of a hydrogen source, A crude oil feed is contacted with one or more catalysts to produce a total product containing a crude oil product 'wherein the crude oil product is a liquid mixture at 25 t and 100 Mpa, the crude oil feed has at least 03 Baitan, the crude oil The feed has an oxygen content of at least 0.001 g of oxygen per gram of crude feed, and the at least one catalyst has a pore size distribution with a median pore size of at least 9GA, which is measured by the ASTM method D4282 ^; and Controlling exposure conditions reduces TAN The crude oil product is made to have a TAN of the crude oil feed having a TAN of up to 90%, and the content of organic oxygen compounds is reduced so that the crude oil product has an oxygen content of the crude oil feed having an oxygen content of up to 90% Among them, ταν is determined by AS ™ method D664, and oxygen content is determined by ASTM method 趵 85. The present invention also provides a method for producing crude oil products, which includes: contacting crude oil with-or more Medium to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at said and 0.11 Mpa, and the crude oil feed has at least (M @ TAN, the at least one catalyst per gram of catalyst In the medium, one or more metals containing one or more metals of the sixth table of the Periodic Table or one or more compounds thereof, or a mixture thereof, containing at least 0.001 g of the appendix of the Periodic Table, based on the weight of the metal; and controlled contact; and The conditions are such that the liquid space velocity in the contact zone is ㈣10h ... and that the crude oil product has a TAN of 90% of the crude oil feed, where ταν is determined by Mm method D664. The present invention also provides a crude oil product Method 'which includes: contacting a crude oil feed with one or more catalysts under a chlorine source to produce a total production γ # A ^ ^ containing a product of crude oil 13 200532010 wherein the crude oil product is at 25.0 and 0.101 MPa The following is: "." 'The crude oil feed has at least 0.1 TAN, the crude oil is fed into each claw, and at least 0.01 g of sulfur per gram of crude oil is fed. 3 One or more metals in column 6 of the periodic table, one or more compounds of metals or columns in the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil feed sucks a knife at a selected rate during the contact period Hydrogen is used to suppress the phase separation of the crude oil feed during the contact, to make the liquid space velocity in multiple contact zones exceed ^ Oh-1, so that the crude oil product has a TAN of the crude oil feed with a TAN of 9G% at most, and The original product has a sulfur content of 70 to 130% of the crude oil feed. The a and t dice cuts are determined by ASTM method D664, and the sulfur content is measured by ASTM method D4294. The present invention also provides a method for producing a crude oil product, which includes: 'contacting a crude oil feed with one or more catalysts to produce a total product containing crude oil production in the presence of a gaseous hydrogen source' wherein the crude oil product is 纟 25 ° C And G.HH MPa is a liquid mixture; and controlling the contact conditions so that the crude oil feed absorbs hydrogen at a selected rate during the contact period to inhibit the crude oil feed during the contact period. The present invention also provides a method for producing a crude oil product, This includes: when one or more catalysts are present, contacting the crude oil feed with hydrogen to produce, 10] ... the compound; and controlling the contact conditions so that the crude oil feed is under the first -I absorption conditions and then It is in contact with hydrogen under the second hydrogen absorption condition. The third absorption condition is different from the second hydrogen absorption condition. Control the first hydrogen absorption condition = hydrogen 14 200532010 to prevent the crude oil feed / total product mixed value from being reduced to 1.5. Below, one or more properties of the crude oil product are changed by up to 90% compared to the individual properties of the crude oil. The present invention also provides a method for producing a crude oil product, which comprises contacting a crude oil feed with one or more catalysts at a temperature, followed by contacting at a temperature of: to produce a total product containing a crude oil product, ^- fr. π 1Λ1 Eight T 5 Hai crude oil product is less liquid at 25 c and 0.101 Mpa 0 ταμ Guan Qiao crude oil feed has a TAN of ·, and control the contact conditions so that the first contact 接触 second contact temperature "then m less Below the feed of the crude oil product with the crude oil

In comparison, with a maximum of 90% TAN, N

Assay D664. TAN is also provided by ASTM. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 2 S η γ μ λ > τ π is a liquid mixture initially at 25 c and 0.101 MPa, 誃 — ^ 0.25. Butan AN, the crude oil feed has a sulfur content of at least 0.0000nj per gram of crude oil feed "Ancient", ten masters / 0.0001 grams of sulfur, "the at least one catalyst contains the sixth or more metals of the periodic table, one or more compounds of one or more metals of the periodic table," or a mixture thereof; And control the contact conditions so that the crude oil product has #TAN of at most $ 90% of the TAN of the crude oil feed and the crude oil product has a sulfur content of 70 to the corresponding sulfur content of the crude oil feed, where TAN It is measured by ASTM method D664, and the sulfur content is measured by ASTM method D4294. Ben Maoming also provides a method for producing crude oil products, which includes: contacting a crude oil feed with-or various catalysts to produce crude oil containing Total product of products, 15 200532010 The product is a liquid mixture at 25t; and 0.101 MPaT is a liquid mixture, the = oil feed has a TAN of at least 0.1, the crude feed has a residue content of at least 0 "grams of residue per gram of crude feed, the at least one The catalyst contains one or more metals of the sixth table of the Periodic Table, one or more of the metals of the periodic table-or more compounds, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a TAN of up to 90% The crude oil feed spoon TAN, so that the crude oil product has a residue content of the crude oil feed to the process, where TAN is determined by the ASTM method and the residue content is determined by the ASTM method. D5307 determination. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing the crude oil product, wherein the crude oil product is a liquid mixture at 2rc and 0.101 MPa, which: The oil feed has at least o " TAN, the crude oil feed has vg0 containing at least 」0" grams of VG per gram of crude oil feed, and the at least one catalyst ^ contains one or A plurality of metals, one of column 6 of the periodic table or one or more compounds of a metal, or a mixture thereof; and an AN 'that controls the contact strips so that the crude oil product has a TAN of up to 90% of the crude oil feed. The crude oil product has a VG0 content of 70 to the crude VGO content of the crude oil = wherein the VG0 content is by A method. The present invention also provides a method for producing a crude oil product, including: The catalyst is contacted to produce a total product containing a crude oil product, which is a liquid mixture at 25t and 0.11 Mpa.

The crude oil feed has a TAN 1 1AN of at least 0. The at least one catalyst can be used by the following 16 200532010 to make the carrier and the column 6 of the periodic table-or more metals, the periodic table two = one or more compounds of one or more metals. , Or a mixture thereof to produce a catalyst driver; in the presence of one or more sulfur compounds

Before heating this catalyst at a temperature of ::::, know the remainder so that the crude oil product has a TAN feed TAN. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product; .1 () is a liquid mixture at 1 MPa, the crude oil feed has a viscosity of at least 10 cSt at 37_rc (10 (rF), the source: from the feed: has an API specific gravity of at least 10, the at least one catalyst Containing the sixth or more metals of the periodic table, the sixth or more metals of the periodic table—or multiple compounds' or mixtures thereof; and controlling the contact conditions so that the crude oil product has the highest viscosity at 纟 37.rc 90% of the crude oil feed is at a viscosity of 37.8. (:, And the crude product has an Aρ specific gravity of 70 to 130% of the crude feed, wherein the Aρ specific gravity is determined by ASTM method D6822 The viscosity is measured by the ASTM method of 669. The present invention also provides a method for producing a crude oil product, which comprises: contacting crude oil, a raw material or a catalyst to produce a total product containing a crude oil product, wherein the crude oil Product at 25 ° C and 0.101 MPa It is a liquid mixture. The crude oil feed has a TAN of at least 0. The one or more catalysts include: one or more catalysts containing vanadium, one or more vanadium compounds, or mixtures thereof; only additional catalysts, wherein the The additional catalyst contains one or more 6th metal, 17 200532010 or one or more compounds of the 6th metal, or a combination thereof; and control of contact equipment so that the crude oil product has a TAN of up to 90% The Ding AN of the crude oil feed, of which TAN is determined by the 8-8 method d664. The present invention also provides a method for producing a crude oil product, which includes: contacting the crude oil feed with one or more catalysts to produce crude oil containing The total product of the product, wherein the crude oil product is a liquid mixture at 25 MPa and 0.11 MPa, the crude oil feed has a TAN of at least 0.01; hydrogen is produced during the contact; and the contact conditions are controlled so that the crude oil The product has a TAN of up to 90% of the TAN of the crude oil feed, wherein the TAN is determined by the method 八. The invention also provides a method of producing a crude oil product, which includes: Match To produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture in the pit and MPaT, the source: the material has at least 0❸ TAN, the at least one catalyst contains vanadium, or a vanadium compound, or a mixture And control the contact conditions so that the contact degree is at least 200 ° C, so that the crude oil product has a TAN of at least 90% of the TAN crude oil feed, where TAN is determined by the astm method DM # °, the present invention A method of producing a crude product is also provided, which includes contacting the crude feed 14 with one or more catalysts to produce a total product containing a crude product, wherein the crude product is a liquid mixture at 25t and 0.11 MPa, The raw feed has a TAN of at least 0, the at least one catalyst contains vanadium, or a vanadium compound, or a mixture thereof; and a hydrogen-containing gas source is supplied during the contact. The gas stream flows as a crude oil feed. Supply in the opposite direction; and control the contact conditions so that the crude oil product has a TAN of the 18 200532010 crude oil feed with a TAN of 90% at most, where TAN is determined by ASTM method D664. Ben Maoming also provides a method for producing crude oil products, which includes: contacting a crude oil feed with one or more catalysts to produce a total product containing crude oil products, wherein the crude oil product is a liquid mixture at 251 and 0.10 MPa, The crude feed has at least 0.00002 grams of total Ni / V / Fe combined per gram of crude feed, the at least one catalyst comprises vanadium, one or more vanadium compounds, or a mixture thereof, and the vanadium catalyst has a median The pore size distribution of at least i80A 'and the contact conditions are controlled so that the crude oil product has a Ni / V / Fe content of the crude oil feed with a total Nϊ / V / Fe content of up to 90%, where Ni / V / Fe content is measured by ASTM method D57708. This gross month also provides a method for producing crude oil products, including: contacting crude oil feedstocks or catalysts to produce a total product containing crude oil products, wherein the crude oil product is liquid at 25t and 0.11 MPa A mixture, the at least one catalyst comprising vanadium, one or more vanadium compounds, or a mixture thereof, the crude feed comprising-or more organic acids-or more metal test salts, one or more organic acids-or alkaline earth metals Salt, or a mixture thereof, the crude oil feed has a total metal and earth metal content in the form of an organic acid metal salt of at least 10,000 grams per gram of crude oil feed; and controlling the contact conditions so that the crude oil The product has the organic acid metal salt form and the total metal content and soil test metal content is "90% of the organic acid metal salt form energy and metal content in the crude oil feed." Metal and alkaline earth metal contents were determined by ASTM method D 3, 8 8. The present invention also provides a method for producing a crude oil product, comprising: contacting a raw material, a feedstock, and-or a plurality of catalysts to produce a total product containing a crude oil product; 19 200532010

Wherein the crude oil product is a liquid mixture at 25 C and 0.11 MPa, and the crude oil feed contains one or more metal salts of one or more organic acids, and one or more alkaline earths of one or more organic acids. Metal salt, or a mixture thereof, the crude oil feed has a total metal and soil test metal content in the form of an organic acid metal salt per gram of crude feed, the at least one catalyst having a median pore control in Pore size distribution in the range of 90 to 1 80 Α, at least 60% of the total number of pores in the pore size distribution has a pore size in the 45 A median pore size range, wherein the pore size distribution is determined by ASTM method D4282; and control Contact conditions so that the crude oil product has a total alkali metal and alkaline earth metal content of up to 90% of the organic acid metal salt form. The organic acid metal salt of the crude oil feed forms an evil alkali metal and alkaline earth metal content, of which the organic acid metal salt The form of alkali metal and alkaline earth metal content was measured by ASTM method D318.

The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25t: and O.HH MPa The crude oil feed has a total Ni / V / Fe content of at least 0.002 g per gram of crude oil feed, and the at least one catalyst has a pore size distribution with a median pore diameter ranging from 刈 to A In the pore size distribution, at least the total number of pores in the pore size has a pore size in the 45 A median pore size range, wherein the pore size distribution is determined by ASTM method D4282; and the contact conditions are controlled so that the crude oil product has a total V / The similar content of the crude oil feed with an Fe content of up to 90%, and its Nl / V / Fe content was determined by ASTM method D5708. The invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with a catalyst to produce a total product containing a crude oil product, wherein the crude oil product is at 25. ^ ± C and MPaT are liquid mixtures. The crude oil feed has at least 0.00001 grams of alkali metal and alkali metals in the form of organic acid metal salts in the parent crude oil. The at least one catalyst has a median The aperture is at least! The pore size distribution of t, 〇A, which is measured by ASTM method D42 82, the contacting θ ^ person "has one or more metals containing the sixth block of the periodic table, the sixth column of the periodic table-Dou, Xi # The pore diameters of α, α, or one or more compounds of metals, or mixtures thereof, can be divided into R'f 'and contact conditions in order to make the crude oil product

The organic acid metal salt can form a total content of alkali metals and alkaline earth metals from a

90% of the crude oil feed has metal and soil metal content, and the content of organic acid metal _ you can be alkali metal and alkaline earth metal in salt form is determined by AST M method D1 3 1 8 determination. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product,

Wherein the crude oil product is a liquid mixture at 2nd generation and 0 · Mpa, the crude oil 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 Mix @, the crude oil feed has a total alkali metal and alkaline earth metal content in the form of an organic acid metal salt per gram of crude oil feed, the at least one catalyst has a median pore size of at least 230A Pore size distribution by ASTM method D4282 'Beijing J 疋, the catalyst has one or more compounds containing one or more metals in column 6 of the periodic table, one or more compounds in column 6 of the week-monthly table, or The pore size distribution of its mixture; and controlling the contact conditions so that the crude oil product has a branched metal salt-shaped metal and soil metal content of up to 90% of the organic acid metal salt form in the crude oil feed The test metal and alkaline earth metal contained 21 200532010, among which the content of alkali metal and alkaline earth metal in the form of metal salt of organic acid was determined by ASTM method D1318. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25 ° C and 0. MPa Is a liquid mixture, the crude feed has a total Ni / V / Fe content of at least 0.00002 grams of Ni / V / Fe per gram of crude feed, the at least one catalyst has a pore size distribution with a median pore size of at least 230A, It is measured by ASTM method 04282, and the catalyst has a pore size distribution comprising one or more metals in column 6 of the periodic table, one or more compounds of one or more metals in the periodic table, or a mixture thereof; and The contact conditions were controlled so that the crude product had a Ni / V / Fe content of the crude feed with a total Ni / v / Fe content of up to 90%, where the Νί / ν /] ^ content was determined by ASTM method D5708. The invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25t and ㈣1 MPa. The crude oil feed contains -Or more organic acids One or more metal test salts, one or more organic acid- or multiple soil test metal salts, or mixtures thereof, the crude oil feed has at least 0 0 0001 grams of alkali metal in the form of an organic acid metal salt per gram of crude oil feed And alkaline earth metal content, the at least one catalyst has a pore size distribution with a median pore size of at least 9GA, as determined by ASTM method D4282. The catalyst has a total molybdenum content per gram of catalyst based on the weight of the catalyst. The amount is between 0.0001 grams and 0.33 grams of ancient dipsticks, 10,000 grams of platinum, one or more compounds, or mixtures thereof; and control contact strips # # # # ”The cow ’s crude oil products have organic acid metals 22 200532010 Alkali and alkaline earth metal content of organic acid metal salt in the crude oil feed with a total content of 9q% of metal and soil metal in salt form. The metal and alkaline earth metal content of organic acid metal salt form is determined by Hunger D 1 3 1 8 was determined. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 0.101 MPa, Material has at least 0.3 # tan and the crude oil feed has a total Ni / V / Fe content of at least 0.00002 grams per gram of crude oil feed, the at least one catalyst has a median pore size of at least AA The pore size distribution of 90A is determined by the astm method D4282. The catalyst is based on the weight of the catalyst per gram of catalyst, and has a total content of 0.0001 to 0.3 grams, one or more types of catalyst. A compound, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a TAN of the crude oil feed with a maximum TAN and the crude oil product has a total Ni / WFe content of up to 90% of the Ni / V / Fe content, JL: The V / Fe content was measured by ASTM ^ 57〇8, and I · was measured by ASTM method D664. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with—or a plurality of catalysts—to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C # 0.101 MPa The crude oil feed contains one or more metal test salts of one or more organic acids,-or multiple organic test salts-or metal test salts, or mixtures thereof. The crude oil = has At least 0 00001 grams of total metal and soil metal content in organic acid metal salt form, the package contains at least 23 200532010 :: one or more metals in the sixth column of the periodic table 'one or more of the six metals in the periodic table -Or more compounds, or mixtures thereof; and weekly: one or more metals of one or more metals of column 10 of the Periodic Table, or mixtures thereof, of the tenth metal The molar ratio of the total amount to the total amount of the metal in column 6 is within the range of ii 1G; and the contact conditions are controlled so that the crude oil product has the total content of alkali metals and alkaline earth metals in the form of metal salts of organic acids. Crude oil feed : Alkali metal and alkaline earth metal content of organic acid metal salt form, the organic acid metal ^ # alkali and alkaline earth metal content ASTm method aspect of the system by DUU measured. The present invention also provides a method of producing a crude oil product, which includes: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0 · 101 MPaT, The crude oil feed has a total Ni / V / Fe content of at least ^ • 00002 grams of Ni / V / Fe per gram of crude oil feed, and the at least one catalyst includes: one or more of ⑷ periodic table f 6 Metal, one or more metals of the sixth table of the periodic table ^ two or more compounds' or mixtures thereof; A (b) one or more metals of the first table of the periodic table, one or more of the metal of the tenth table of the periodic table One or more compounds, or mixtures thereof, in which the molar ratios of the total metal of the 10th metal and the total metal of the 6th column range from 1 to 1G; and controlling the contact conditions so that the crude oil product has a total Ni / V The Ni / V / Fe content of the crude oil feed with a maximum / Fe content of 90%, wherein the NL / V / Fe content is determined by the astm method D5708. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil 24 200532010 feed with one or more catalysts to produce a total product of crude oil products in Block 3, wherein the crude oil product is at 25 ° C and 0.101 MPa τ y ^ It is a liquid cancer mixture at λ MPa. The crude oil feed contains-or more organic acids-or more metal test salts, one or more organic acid-or more soil tests, or a mixture thereof. Gram crude oil feed has a total content of test metal and alkaline earth metal in the form of organic acid metal salt, at least one or more catalysts include: the first catalyst, the first catalyst per gram In the first catalyst, based on the weight of the metal, it contains 0.006 to 0 ′, page 6 of the periodic table of the table.

One or more metals, weekly 6 or more-one or more species of metals: substances' or mixtures thereof; A (b) a second catalyst, the second catalyst at a gram of the second catalyst Medium ', based on the weight of the metal, contains at least 002 grams of one or more metals in Period 6 of the Periodic Table, one or more metals in column 6 of the Periodic Table-or more compounds, or mixtures thereof; and controlling the contact conditions so that The crude oil product has a total metal test and soil test metal content of organic acid metal salt form of up to 4 90% of the alkali metal and alkaline earth metal content of the organic acid metal salt form in the crude oil feed, of which the alkali metal in the form of the organic acid metal salt

The test soil metal content was determined by ASTM method D1318. The present invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. (: And G.1G1 MPa is a liquid mixture, the original / by the feed bag δ or more organic acid one or more metal test salts, one or more organic acid one or more alkaline earth metal salts, or a mixture thereof, the The crude oil feed has a total alkali metal and alkaline earth metal content of at least 10,000 grams of organic acid metal i-formaldehyde per gram of crude oil feed. By weight, containing at least 0.001 g of one or more metals of column '6 of the periodic table, one or more compounds of one or more metals of the periodic table, or mixtures thereof; and controlling the contact conditions so that the contact The space velocity of the liquid in the zone exceeds 101rl, and the crude oil product has the total content of metal and earth metal in the form of organic S, and is the alkali metal and alkaline earth metal in the form of organic acid metal salt in the crude oil feed. The content of alkali metal and alkaline earth metal in the form of organic acid metal salt is determined by ASTM method; 013 1 18. The present invention also provides a method for producing a crude oil product, which includes: The crude oil product is contacted with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, and the crude oil feed has at least 0.00002 grams of total crude oil feed. / FC i i, the at least one catalyst in metal per gram of catalyst contains at least 0.001 grams of one or more metals in column 6 of the periodic table, one or more metals in column 6 of the periodic table Or more compounds, or mixtures thereof; and controlling the contact conditions such that the liquid space velocity in the contact zone exceeds 10 h and the crude oil product has a total content of Nl / V / Fe of the crude oil feed of up to column% φ Content, wherein the Ni / V / Fe content is determined by ASTM method D5708. The present invention also provides a method for producing a crude oil product, which includes: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product The crude oil product of Yizhong 4 is a liquid mixture at 25 C and 0.1 10 MPa, and the crude oil feed has at least 0.0001 grams of oxygen 3 'per gram of crude oil feed. For 0.0001 grams of sulfur, this at least The catalyst includes one or more metals of the 26th period of the 200532010 table, one or more compounds of one or more metals of the 6th table of the periodic table, or a mixture thereof; and controlling the contact conditions so that The oxygen content of the crude oil feed having an oxygen content of at most 90%, and the crude oil product having a sulfur content of 70 to 13% of the crude oil feed, wherein the oxygen content is It is measured by ASTM method E385, and the sulfur content is measured by ASTM method D4294. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil supplier or a catalyst to produce a total product containing crude oil. Product, where the crude product is a liquid mixture at 25t: and G1G1, and the crude feed has a total N: i / V / Fe content of at least 20,000 grams per gram of crude feed, containing sulfur An amount of at least 0.001 g of sulfur, the at least one catalyst comprising one or more metals of cabinet 6 of the periodic table, one or more compounds of one or more metals of periodic table 6, or a mixture thereof; and The contact conditions are controlled so that the crude oil product has a total Ni / V / The Fe content is at most 90% of the Ni kg / Fe content of the crude oil feed, and the crude oil product has a sulphur content of 70 to 130% of the crude oil feed, including ni / The v / fe content is determined by ASTM method D5708, and the sulfur content is determined by astm method D4294. 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 containing a crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the The crude oil feed contains one or more alkali metal salts of one or more organic acids, one or more earth test metal salts of one or more organic acids, or a mixture thereof. The crude oil feed has at least 0.00001 grams per gram of crude oil feed. Organic acid metal 27 200532010 The total content of alkali and alkaline earth metals in salt form and a residue of at least 0.01 g of edging. The at least one catalyst contains one or more of the subordinates in column 6 of the periodic table. One or more compounds of one or more metals in column 6, or a combination thereof, and controlling the contact conditions so that the crude oil product has an organic meaning to a salt form, and the total content of alkali metals and alkaline earth metals is at most for the crude oil. The content of alkali metals and alkaline earth metals in the form of metal salts of organic acids in the feed, and the crude oil product has a residue content of 70 to 130% of the crude oil content The metal content and metal content of the organic acid metal salt are determined by ASTM method Dm8, and the residue content is measured by AST1V [method D5307. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25t; and a liquid mixture at 0.101 MPa, the The crude oil feed has a residual content of at least 0.1 g per gram of crude oil feed, a total Ni / V / Fe content of at least 0.00002 g, and the at least one catalyst, including —Or more than one metal, one or more compounds of the more than one metal ”or a mixture thereof; and controlling the contact pieces so that the crude oil product has a total Ni / v / Fe content of up to 90%, the ^ The Nl / V / Fe content is fed, and the crude oil product is made to have a residue content of 70 to 13% of the residue of the crude oil feed.

Ni / V / Fe ^ λ ^ τ is determined by ASTM & D57〇8, and residue hunting is determined by ASTM D53〇7. The feedstock also provides a method of producing a crude oil product 'which comprises: contacting a crude oil core,-or a plurality of catalysts to produce a total product containing a crude oil product, 28 200532010 wherein the crude oil product is ancient 9 ς. The substrate is a liquid mixture at 25C and 0 · 101 MPa. The crude oil feed order is less than 1% S or one or more alkali metal salts of organic acids, or one or more alkaline earth metals of organic I.胄, or a mixture thereof, the crude oil feed has at least 0.1 i vacuum gas oil ("VGO") in the mother gram crude feed containing |, π ηΑΛ1 ^ in the form of a metal salt of organic acid of 0.0001 g Alkali metals and •, genus ,,, and 3, the at least one catalyst includes one of the sixth block of the periodic table

= Multiple metals '-column 6 of the periodic table-or multiple metals-or multiple compounds' or mixtures thereof; and controlling the contact conditions so that the crude oil product possesses it. The total content of alkali metal and alkaline earth metal in the form of organic acid metal salt is at most 920, and the content of alkali metal and alkaline earth metal in the form of organic acid metal salt in the crude oil feed, and the crude product has a VG content of 70 to The VG0 content of this crude oil feed was 130%, where the VGO content was determined by AStm method D5307, and the alkali metal and alkaline earth metal content in the form of metal salts of organic acids were determined by ASTM method D1318.

The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at a temperature of 0.001 and 0.001 Mpa The crude oil feed has a total • / V / Fe §i of at least 0.0002 grams per gram of crude oil feed, a vg0 content of at least 0.1 grams, and the at least one catalyst comprises the first One or more metals, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a total Ni / V / Fe content of up to 90% The Ni / V / Fe content of the crude oil feed, and the crude oil product has a vg0 content of the crude oil feed with a VG0 content of 70 to 130%, of which the VGO content is 29 200532010 by the ASTM method D5307 The Ni / V / Fe content was measured by ASTM method D5708. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25 ° C. . And a liquid mixture at 0.101 MPa, the crude oil 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 a mixture thereof. A gram of crude oil feed has a total alkali metal and alkaline earth metal content in the form of a metal salt of an organic acid of at least 10,000 g. The at least one catalyst can be obtained by using a carrier and one in column 6 of the periodic table. One or more metals, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof to produce a catalyst precursor, which is heated at a temperature below 400 C in the presence of one or more sulfur-containing compounds A catalyst precursor to form a catalyst; and controlling the contact conditions so that the crude oil product has an alkali metal and alkaline earth metal content in the form of organic acid metal salt in a total amount of 90% of the alkali metal in the form of organic acid metal salt in the crude feed And alkaline earth metal content, where the organic acid metal salt forms your alkali metal and alkaline earth metal content are determined by the ASTM method. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed person or a catalyst to produce a total product containing a crude oil product, wherein the crude oil product at 25 ° C and 0-10.1 MPa is Liquid mixture, the crude feed having a total Ni / V / Fe content of at least 200000 grams per gram of crude feed, the at least one catalyst can be obtained by: One or more metals that are blocked, one or more of the 30th column of the Periodic Table of the 2005 20052010 metal or compounds or mixtures thereof to produce a catalyst precursor; in the presence of one or more sulfur-containing compounds, at less than The catalyst precursor is heated at a temperature of 400 t to form a catalyst; and the contact conditions are controlled so that the crude oil product has a total Nl / V / Fe content of 90% Ni / V / Fe of the crude oil feed Contains $, where Ni / V / Fe content is determined by the astm method⑽. The present invention also provides a crude oil composition containing the following in each gram of crude oil composition. At least 0.001 grams of a hydrocarbon having a boiling range distribution between 95 ° C and 26 ° C at 0,001 MPa; at least 0.00. 〇1 gram boiling range distribution of hydrocarbons between 26GC and 320 ° C under 〇ιιιο; at least 〇! ⑻! Gram boiling range distribution between 320. MPa at 0. 101 MPa. (: And 65GX: Hydrocarbons; and one or more catalysts containing more than 0 g, but less than 0.01 g per gram of crude oil product. The present invention also provides a crude oil composition containing at least one of the following per gram of crude oil composition. 0.001 g of sulfur, determined by astm method D4294; at least 0.2 g of residue, measured by ASTM method D5307, the composition has a weight ratio of MCR content to c5 asphaltene content of at least 1.5 The MCR content is determined by ASTM method 0453〇, and the q asphaltene content is determined by ASTM method D2007. The present invention also provides a method for producing a crude oil product, which includes: crude oil feed and one or more catalysts Contact to produce a total product containing crude oil products, "Medium 4 crude oil products at 2 5 C and 0.1 0 1 Condensable at MPa, the crude feed has an MCR content of at least 0.001 grams per gram of crude feed, and the at least one catalyst can be obtained by: Or more than one metal, one or more compounds of one or more metals in the sixth table of the Periodic Table 31 200532010 compound 'or a mixture thereof to produce a catalyst precursor sulfur compound in the presence of low ☆ 5GGt warm or evening species containing AL ^ Λ > gn…, the catalyst precursor sacrificial catalyst; and the contact conditions to control the MCR content of the crude oil feed with a crude oil content of up to 4 90%, where '_containing 1 is determined by ASTM method D4530 Qiao

The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is condensable at 25 t and 0.11 purchase The crude feed has an Mcr content of at least 0.001 grams per gram of crude feed, the at least one catalyst has a pore size distribution with a median pore size ranging from 70 to 180 people, and the pore size distribution At least 60% of the total number of pores has a pore size in the median pore size range of 45 people, where the pore size distribution is determined by the astm method D4282; and the contact conditions are controlled so that the crude product has an mcr of 90% at most The MCR of the crude feed, where MCR is determined by the α§τμ method D45 30. The present invention also provides a crude oil composition containing the following in each gram of composition: up to 0.004 grams of oxygen, as measured by ASTM method E385; up to 0.003 grams of sulfur, as measured by ASTM method D4294; and at least 0.3 g of residue as determined by AST1V [Method D5307. The present invention also provides a crude oil composition containing the following in each gram of composition: up to 0.004 g of oxygen, as measured by ASTM method E385; up to 0.003 g of sulfur, as measured by ASTM method D4294; up to 0.00. 4 grams of experimental nitrogen, determined by ASTM method D2896; at least 0.2 grams of residue, measured by ASTM method D5307; and the composition has a maximum of 32 200532010 TAN, which is more than 0.5 Assay D664. The present invention also provides a crude oil composition containing the following in each gram of composition: at least 0.001 grams of sulfur, measured by ASTM method D4294; at least 0.2 grams of residue, measured by ASTM method D5307; the composition The weight ratio of MCR content to c5 asphaltene content of 1.5, and the composition has a TAN of up to 0.5, where TAN is measured by ASTM method D664, and the weight of MCR is measured by ASTM method D4530 The weight of I asphaltene was measured by ASTM method D2007. In several specific examples, the present invention and one or more of the methods or compositions of the present invention also provide the following crude oil feeds ... (a) those that have not been processed in a refinery, steamed and / or fractionated; contain carbon For components with a number greater than 4, the crude oil feed contains at least 0.5 grams of this type of feed in each gram of crude oil feed; (c) contains hydrocarbons, some of which have: less than 10 at 0.1 MPa The boiling range distribution of 〇t is between 100 ° C and 200 at 0.101 MPa. A boiling range distribution between 〇, a boiling range distribution between 200 ° C and 300 ° C at 0.101 MPa, a boiling range distribution between 300 ° C and 400 ° C at 0.101 MPa, and Boiling range distribution between 400 ° C and 650 ° C at 0.101 MPa; spring (d) contains at least · 0 · 001 grams per gram of crude oil feed with a boiling range distribution below 0.101 MPa 〇〇. 〇hydrocarbons, 0.001 grams of hydrocarbons with a boiling range distribution between 0.1 ° C and 200 ° C at 0.101 MPa, 〇_〇〇01 grams of hydrocarbons with a boiling range distribution at 0.101 MPa and 200 ° C and Hydrocarbons between 300 ° C, 0.001 grams of fumes with a boiling range distribution between 0.1 ° C and 300 ° C at 0.101 MPa, and 0 · 〇0 1 grams of fumes with a boiling range distribution of 0.1 1 〇1 Hydrocarbons between 400 ° C and 650 ° C at μ pa; (e) have at least 0 ″, less than 33 200532010, or 0.3, or 0.3 to 20 ′ 0.4 to 10, or 0.5 TAN in the range of $; (f) has a starting point of at least 2000c at 0.11 MPa, (g) contains iron, hunger, and iron, (h) per gram Crude feed contains at least 0.00002 grams of total N " V / Fe; ⑴ contains sulfur; ⑴ contains at least 0.0001 grams or 0.05 grams of sulfur per gram of crude feed; (k) contains at least 0.001 grams of sulfur per gram of crude feed 0.001 grams of VGO; (1) contains at least 0.1 grams of residue per gram of crude feed; (m) contains oxygenated hydrocarbons; (n) one or more alkali metal salts of one or more organic acids, one or more One or more alkaline earth metal salts of organic acids Or mixtures thereof; (square) comprising at least one organic acid salts speech; and / or (p) comprising at least one organic acid salt Shi Shen. In several specific examples, the present invention and those combining one or more methods or compositions of the present invention also provide crude oils that can be obtained by removing naphtha from crude oil and compounds more volatile than naphtha. Feed. In several specific examples, the present invention and a combination of one or more methods or compositions of the present invention are also & a method for contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil Both the feed and crude product have C5 asphaltene content and MCR content, and · r, • The sum of the C: 5 cyanide content of crude oil feed and the MCR content of crude oil feed is s, and the C5 pitch of crude oil product is The sum of the mass content and the MCR content of the crude oil product is S ′, and the contact conditions are controlled so that S ′ is at most 99% of S; and / or (b) the contact conditions are restrained so that the CR CR content of the crude product and the crude product ^ The weight ratio of the cyanine content is in the range of 1.2 to 2.0, or 1.3 to 1.9. 5 In some specific examples, the present invention and a combination of one of the present invention to take a variety of methods or compositions also provide a hydrogen source, The hydrogen source is: (a) gas energy (M 34 200532010 hydrogen; (C) pinane; (d) light hydrocarbons; (e) inert gas; and / or tritium mixtures thereof.) In several specific examples, the present Inventions and combinations of the invention—or methods or compositions are also mentioned A method of contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, where the crude oil feed is contacted in a contact zone located or connected to an offshore facility. In a number of specific lifelines, The present invention and those combining one or more methods or compositions of the present invention also provide a method comprising contacting a crude oil feed with one or more catalysts in the presence of a gas and / or chlorine source and controlling the contact conditions in order to make · (A) The ratio of gaseous hydrogen source to crude oil feed is in the range of 5 to 800 standard cubic meters of gaseous hydrogen source per cubic meter of crude oil feed in contact with one or more catalysts; (b) The selected net uptake of argon is controlled by changing the partial pressure of the hydrogen source; (c) The uptake of hydrogen makes the crude oil product have an AN less than 0.3, but the uptake of hydrogen is less than that during the contact will cause crude oil feed and The amount of hydrogen uptake through the phase separation between the total products; (d) The selected hydrogen uptake rate is within the range of 1 to 30 or 1 to 80 standard cubic meters of hydrogen source per cubic meter of crude oil feed; e) The liquid space velocity of the gas and / or hydrogen source is at least 11 ^ At least 15 h ·], or at most 2 0 ^; 控制 control the partial pressure of the gas and / or hydrogen source during the contact; (g) the contact temperature is in the range of 50 to 5001, the total of the gas and / or hydrogen source The space velocity of the liquid is in the range of 0.1 to 30 h_], and the total pressure of the gas and / or hydrogen source is in the range of 10 to 20 MPa. (H) The flow of the gas and / or hydrogen source is toward The direction opposite to the flow of the crude oil feed; (i) the crude oil product has an H / C of 70 to 130% of the H / C of the crude oil feed; (j) the hydrogen absorbed by the crude oil feed per cubic meter of 35 200532010 The crude oil feed has a range of up to 80 and / or i to 80 or i to 50 standard cubic meters of hydrogen; (k) the crude product has a total Ni / V / Fe content of up to 90% and up to The Ni ~ / Fe content of the crude oil feed is 50% 'or up to 10%; (!) The crude oil product has a sulfur content of 70 to 130% or 80 to

The sulfur content of the crude feed; (m) the crude product has a VGO content of 70 to 130% or 90 to 110% of the crude to a 13% or 9 feed VGO content; (n) the crude product Has a residue content of the crude oil feed of up to M%; (0) the crude oil product has an oxygen content, mostly 90%, up to 70%, up to 50%, up to 40% , Or up to 10〇 /. The oxygen content of the crude feed; (p) the crude product and yes. The total content of alkali metals and alkaline earth metals in the form of organic acid metal salts is at most 50 / 〇, or at most $! 〇% of the organic acid of the crude oil feed

Contents of alkali metals and alkaline earth metals in the form of metal salts; (q) during the contact, the crude oil feed has a P value of at least ⑴; ⑴ the crude oil product has a viscosity of up to 9G% at 378 C, or Up to 10% of the viscosity of the crude oil feed at 37. generation; ⑷ the crude oil product has an Aρι specific gravity of 70 to 130% of the crude oil feed; and / or cough = the product has the most TAN It is 90%, maximum 50%, maximum response, 20%, or 10% of the crude oil feed. One to one. .2, or. .…In the range. In several specific examples, the present invention and a combination of one or more of the present invention or a composition also provide a method comprising contacting a crude oil feed with one or two catalysts and controlling the contact conditions to reduce organic oxygen compounds (A) 'Select the content of 疋 organic oxygen compounds so that the 36 200532010 crude oil production has the oxygen content of the crude oil feed with the maximum oxygen content of ㈣%; At least one of the compounds contains a metal salt of a carboxylic acid; at least one of the organic oxygen compounds includes an alkali metal salt of a carboxylic acid; (d) at least one of the organic oxygen compounds includes a carboxylic acid Alkaline earth metal ⑷ At least one compound containing organic oxygen compounds ㈣ Gold stomach including ㈣ of the periodic table-or more metals; ⑴ The crude oil product has a crude oil feed containing a non-carboxylic acid organic compound content of up to 90% Content of non-acidic acid-containing organic compounds; and / or at least one oxygen-containing compound in the crude oil is produced from naphthenic or non-carboxylic acid-containing organic oxygen compounds. In several specific examples, the present invention versus A method is also provided in combination with one or more methods or compositions of the present invention, which comprises contacting a crude oil feed with a catalyst, wherein the crude oil is fed to the-at the-temperature;- This kind of catalyst is contacted, and then contacted at the second temperature, the control contact, 1 卞: Second, the first contact temperature is at least 30 ° c lower than the second contact temperature; (b) Fang; under the conditions of wind absorption Under the second chlorine absorption condition, the crude oil feed is brought into contact with hydrogen, and the temperature of the first absorption condition is at least lower than the temperature of the second absorption condition ㈣, (the crude oil is fed at the first temperature "to ^ Catalyst contact 'followed by contact at a second temperature to control contact

The condition X makes the first contact temperature lower than the second contact temperature. C. The bucket is produced during the contact period. G ^ The raw wind milk, (e) Hydrogen is generated during the contact period, and the contact conditions are restrained so that the crude oil feed absorbs at least a part of the generated chlorine m from the feed and the first and the first. Two kinds of catalysts are contacted. The contact of the first catalyst of the crude oil feed tray generates an initial crude oil product, wherein the initial crude oil product has 37 200532010 TAN with a maximum of 90% of the crude oil feed in the μ device; h) Fang Fang's "(g) Fang; the reactor bed reflects the contact of the crude oil feed in the toilet, (1) the one or more contacts A such as fine *, force catalyst contact, (j ) The catalyst is a vanadium catalyst. After the crude oil is brought into contact, at _ ,, and 6 + 10, after each contact with the catalyst, and with the presence of a wind source, it will contact the additional catalyst with a square meter of crude oil feed 1 to? Λ Divine. Live) Fengxin produces 4 · m within a range of quasi-cubic cubic meters of the mother's ice moraine, and produces 氲 during the contact period, which is produced in the air carving # ^ 丨 〇 逑 leather, (I) The existence of hydrogen generated by a part of the limb father makes θ the original, and feeds and attaches to make the gas flow toward the disk material '"and control the contact conditions to; The second step is to make the reaction and the ammonia flow opposite. The second is that the oil feed is in contact with the catalyst at the first temperature, and then the temperature is at least lower than the first contact. The crude feed became more attached ... Guangxi produced hydrogen during the contact, and the catalyst absorbed at least-part of the contact conditions in order to make the attachment under the condition; f, lice, and / or (〇) subsequently at a second temperature The second temperature is at least 180t. "Touch 'to control the contact conditions so that a number of specific examples and methods can be used in conjunction with the present invention-or multiple times, and the creator also provides one or more catalyst contacts, where ... Shanshan crude oil feed and-containing Alumina, oxidized stone 亥 a 'Hai catalyst is a loaded catalyst and the carrier encapsulates magnesium, ^ # silica-alumina, titanium oxide, banknote oxide, oxygen

The chemical properties of Huazhen, or its mixture of semi-goat sheep; (c) this square catalyst is a loaded catalyst and the carrier is a porous treated additional catalyst; (d) at; ^ not already higher than · c The temperature is below the year; and the heart) ： at least-: the life of the two catalysts is at least °. 5 catalysts are in a fixed bed or suspended in the original 38 200532010 oil feed. In the specific example of the right stem, the present invention and the method or composition combining the present invention are also provided with one or more methods, which include contacting crude oil or a variety of catalysts. Medium or massive two-type catalyst 'The loaded catalyst or massive metal catalyst: ⑷ & Contains metals 5 to 10 of the periodic table-or more metals, columns 5 to 10 of the periodic table-or more Metallic- or multiple compounds, or mixtures thereof; (b) containing at least 0.0001 g, 0.0001 to 0.6 g, or 0.0001 to 0.3 g per gram of catalyst: 5 to 6 of the periodic table One or more metals in column 10, 5 to 周期 of the periodic table-one or more compounds of metals, or mixtures thereof; ⑷ containing columns ^ 6 to 1G-or more of metals in periodic table 6 to 10 One or more compounds of one or more metals, or mixtures thereof; one or more metals including columns 7 to 10 of the work table, 7 to 8 of the periodic table—or one or more compounds of multiple metals, or Mixture; ⑷ in: gram catalyst contains 0.0001 to 0.6 g or 0.001 to 03 g: week j: 7 1〇 bar one or more metals of the Periodic Table of the column 7 to metals or evening - or more compounds, or mixtures thereof,

Period 矣 # C ^: One or more metals from 6 to 6, and from week 5 to 6 of the periodic table: multiple metals—or multiple compounds, or mixtures thereof; ⑻ contains = Table 5—or more Metals, column 5 of the periodic table—or more than three compounds, or mixtures thereof; ⑻ per gram of catalyst: at least 〇〇〇〇 (Η g, 〇._ to 0.6 g, 〇〇〇〇 1 to 0.03 grams, 0.005 grams, or 0.01 to 0.08 grams: one or more Meng in column 5 of the periodic table-'f 5 in column-or more metals-or more Compound, 39 200532010 or something thereof; ⑴ contains the sixth block of the periodic table-the cousin of the period 6-or more of the metal-or a variety of metal, the weekly matter; 含有 per gram of the catalyst contains 〇00〇ι To 〇 °, or its mixed gram, 0.005 to (M gram, 〇 •• '0.001 to 0.3 ri · υ8 gram cycle 妾 or more metals, the sixth table of the periodic table-or a combination of 6 , Or a mixture of them; bag, * genus-or a variety of genus, leisurely as the main column of the periodic table brother W column of the eight genus' periodic cousin 10 ㈣- One or more of a variety of metals: from the heart to 03 grams. There are 0.0001 to 0.6 grams or _ grams of the-or more metals of the Periodic Table, 10th, the compound of the 10th order of the periodic table, Or a mixture thereof; (m) containing vanadium, one or more vanadium compounds, sub-eight compounds; (η) containing nickel, one or more compounds, or mixtures thereof; ⑷ containing cobalt,-or multiple compounds, or mixtures thereof (P) contains molybdenum,-or more molybdenum compounds, or mixtures thereof; (i) contains 0.001 to 03 grams or 0 005 to 0.1 grams per gram of catalyst: molybdenum, one or more molybdenum compounds, or Mixtures; (Γ) containing 3 tungsten '-or more crane compounds, or mixtures thereof; rhenium at 0.001 to 0.3 g per gram of catalyst 3: tungsten, one or more tungsten compounds' or mixtures thereof; ⑴ & with periodic table The one or more metals of the diaphragm and the metal of the periodic table—or more than one metal, in which the molar ratio of metal 1G to metal in column 6 is 1 纟 5 '⑷ contains one or more elements of the fifth shed of the periodic table , One or more compounds of one or more elements in column 5 of the periodic table, or a mixture thereof; Each gram of the catalyst contains 0.001 to 006 grams of: one or more elements of one or more week / monthly table of one element, one or more compounds of column 15 of the periodic table, or Mixtures; (w) phosphorus, one or more 40 200532010 phosphorus compounds, or mixtures thereof; A > Primary (X) contains up to 0 g of (X alumina) in the master gram catalyst and / or (y) in each The ancient Fenhuo Shangshan people contain at least 0.5 alumina in the mother catalyst. In some specific examples, the present invention and a combination of one or more methods or compositions of the present invention also provide a method for forming a catalyst. , # Including the carrier combined with or a metal to form Du Zhuan / Mo Li ~ Feng war body / metal mixture, wherein the carrier contains Θ oxidation | Lu, at least 400, 6, sore πτPrivate buckle η ρ L is heat-treated at a degree of 0 ° alumina support / metal mixture, and it also includes ⑷ to make the support / metal mixture and water company into a paste, squeeze this paste; (b) at least 8 〇〇t's temperature: θ oxidized by heat treatment of alumina,... ^ Fu emulsion Ming, and / or (c ) The catalyst is vulcanized. In several specific examples, the present invention and one or more of the present inventions are combined with one another, and the creator also provides a method comprising contacting a crude oil feed with one or more catalysts, wherein the-or more catalysts Has a pore size distribution of at least 60A, at least 90A, at least 18Oa, at least 200A, at least 230A, at least 300A, at most 23A, and at most 500A , Or in the range of 90 to 180 A, 100 to 140 A, 120 to 130 A, 230 to 250 A, 180 to 500 A, 230 to 500 A; or 60 to 300 A Position hole shuttle; (b) at least 60% of the total number of holes has a pore size in the range of 45A, 35A, or 25 in the median pore size; (c) at least 60 m2 / g, to) 90 m2 / g, A surface area of at least 100 m2 / g, at least 120 m2 / g, at least 50 m / g 'at least 200 m2 / g, or at least 220 m2 / g; and / or (d) at least 0 · The total volume of all pore sizes of 3 cm3 / g, at least 0.4 cm3 / g, at least 0.5 11 / g 'or at least 0.7 cm3 / g. 41 200532010 In several specific examples, the present invention and the combination of the present invention-or multiple methods or compositions also provide a method comprising contacting a crude oil feed with one or more supported catalysts, A3 halberd beans · (a) contains aluminum oxide, stone oxide, stone oxide-aluminum oxide, titanium oxide, hafnium oxide, magnesium oxide, or a mixture thereof, and / or zeolite; (b) Bai Yaoer 々, package 3 yaluminum alumina and / or δ alumina; (c) 3 to 彡 0.5 g of γ alumina in a person's load; ⑷ 3 at least 0.3 g per gram of carrier or Up to 205 grams of yttrium oxide; y < containing oxide, γ alumina, δ gasification button, ^ aluminum θ aluminum oxide, or mixtures thereof; (f) in each

The gram carrier contains up to 0.1 grams of alpha alumina. In some specific examples, the present invention and a combination of one or more of the present invention also provide a vanadium catalyst: ⑷ pore distribution from a median pore size to 60A; This carrier contains tritium oxide and Lu ', and the nuclear catalyst has a pore size distribution with a median pore size of at least 6GA; Or more compounds, or mixtures thereof; and / or rhenium containing at least 0.001 g per gram of catalyst: one or more of the 6th table

Species # 6 of the Periodic Table—or multiple metals—or multiple compounds, or mixtures thereof. In some specific examples, the present invention and those who combine one or more methods or compositions of the present invention also provide a crude oil product, which has a maximum of 1 0.001 to 0.005 '0.01 to 0.2; or 0.05 to 0.2. TAN of J; Less ... Alkali metals and alkaline earth metals in the form of organic acid metal salts of up to 9000 g per gram of crude oil product; (c) Up to • 0002 g of Ni / g per gram of crude oil product V / Fe; and / or (d) at least one catalyst greater than 42 200532010 0 g, but less than 0.01 g per gram of crude product. In some specific examples, the present invention and one or more methods or compositions combining the present invention also provide one or more alkali metal salts of one or more organic acids, one or more organic acids • or]] Alkaline earth metal salts, or mixtures thereof, of which: (a) the at least one species is a bell, sodium, or potassium; and / or (b) the at least one alkaline earth metal is magnesium or calcium. In several specific examples, the present invention and those combining one or more methods or compositions of the present invention also provide a method comprising contacting a crude oil feed with one or more catalysts to produce a crude oil product containing The total product of this method further includes: (i) combining the crude oil product with the same or different crude oil feed to form a blend suitable for transportation; (b) making the crude oil product the same as the crude oil feed Or different; ^, combined with Shantou NH 扪 crude oil to form a blend suitable for processing equipment; (c) fractionating the crude product, field products, and / or (d) fractionating the crude product I remains as one or more distillates, and at least one distillate is used to produce transportation fuel from Mori. In some specific examples, the present invention and those who combine one or more methods or compositions of the present invention also provide a supported catalyst composition, which: (a) contains at least 0.3 g or at least 0.05 g in a mother gram carrier Θ alumina 丨 ⑼ contains δ alumina in the carrier; 含有 contains a maximum of 0.01 g of α oxide per gram of the carrier; ⑷ has a pore size distribution with a median pore size of at least ⑽; pores with the pore size distribution Porous bodies of at least G.3 em3 / g or at least ^ have a surface area of at least 60 m2 / g or at least 90 m2 / g; ω contains one or more metals in the seventh to tenth of the periodic table, and seventh in the periodic table To one or more compounds of columns 10 to 10 or more, or mixtures thereof; 43 200532010 (\, two or three metals of the third periodic table, one or more compounds of column five or more of the periodic table , Or a mixture thereof; 含有 in each gram of catalyst 〇βΛΓη xi 'ϋ · 0001 to 0.6 g or 0.001 to 0.3 g: one or five kinds of metal,-or more than the fifth column metal compound, or Its mixture (j) consists of one or more metals in Block 6 of the Periodic Table, Block 6 in the Periodic Table One or more compounds of the genus & Mon, or mixtures thereof; (k) 0.00000 s per gram of catalyst, 0.001 to 0.6 g or 0.001 to 0.3 g per gram of catalyst: 1: Column 6 metal,-or multiple Column 6 metal compounds, or mixtures thereof

. The substance '⑴ contains one or more compounds, or mixtures thereof; ㈣ contains molybdenum,-or more molybdenum compounds, or mixtures thereof; ⑻ & contains tungsten, one or more tungsten compounds, 苴, 人, ^ Human body compound; contains cobalt, one or more cobalt compounds, or is mixed in with one's, σ, and / or (P) contains nickel, one or more nickel compounds, or a mixture thereof. In some specific examples, the present invention and those combining one or more methods or compositions of the present invention also provide a kind of crude oil composition, #: ⑷ and there is at most = 1, at most 0.5, at most 0.3, or at most 0. ^ ταν; ⑻

Each gram of composition contains at least 〇. Υ. 001 grams of boiling private distribution between valence and · at 0.101 MPa. Smoke between c; Gu 1, at least 005

The dharma distribution of gram or to /0.01 gram is between dove at 010 MPa. Hydrocarbons between C and 320 ° C; and furnaces with a boiling range distribution of at least 0.001 / ϋ · 00ΐg at 0 · 101 MPa and between 320 ° C and 6500 ° C , (C) contains at least 0.0005 grams of basic nitrogen in the mother gram composition; Yili Liu △ 丄, (d) contains at least 0.0000 grams or at least θ · οι grams of the mother gram composition Total nitrogen content and / or a, and / or 0) contains up to 0.00005 grams of total nickel and vanadium per gram of composition. 44 200532010 In some specific examples, the present invention and those who combine one or more methods or compositions of the present invention also provide a crude oil composition comprising one or more catalysts' The at least one catalyst · (3) has a median The aperture is at least 180 people, and the beam is 500 "/in...........A, ^

Pore size distribution to 130 Λ; (b) has a median pore size of at least 90 A, more than 60% of the total pore numbers in the M pore size distribution have pore sizes in the range of 45 A, 35 A, and 25 j median pore size (C) has a surface area of at least 100, at least 120 m2 / g, or at least 22 m2 / g; (d) includes a carrier;

The support includes alumina, silica, silica-alumina, titania, oxonium oxide, magnesia, zeolite, and / or mixtures thereof; (e) one or more metals containing columns 10 to 10 of the periodic table, the periodic table 5th to 10th _ ^ Dover metal-or more compounds, or mixtures thereof; (f) & containing the first or more metals of the periodic table, one or more of the five metals of the periodic table, One or more compounds, or mixtures thereof; (g " containing at least 0.0001 grams per gram of catalyst: one or more of the fifth column of all or more of the fifth metal compounds, or mixtures thereof; (h) containing ,,

One of the metal 'week_6 columns or the next day species or one or more of the genus Limonis or their mixtures; ⑴ at the mouth of each gram of contact or multiple 6th metal ... or more ^ with at least ⑴: Species 6 metallized characters, compounds; (J) Contains 10 or eight mixed columns of the periodic table-10 or more full ㉟P "metals, the periodic table contains the periodic table The 15th -or matter; and the compound or compounds of one or more elements, the second and the fifth stage of the table 15 In a further specific example, the special feature of the present invention /, and the special feature of the special example 45 200532010 The characteristics may be combined with the characteristics of other specific examples of the present invention. For example, the characteristics of one specific example of the present invention may be combined with the characteristics of other specific examples. In a further specific example, the crude oil product may be obtained by the Obtained by any method and system. In further specific examples, additional features can be added to the specific specific examples described herein. [Embodiment] The specific specific examples of the present invention are described in more detail here. Definitions of terms used herein as follows. "ASTM" means the American Standard for Testing Materials. API specific gravity '' means at 15 5. Aρι specific gravity at 〇 (6〇τ). The absolute specific gravity was measured by ASTM method D6822. The atomic hydrogen percentage and atomic carbon percentage of crude oil feeds and crude products are determined by ASTM method D5291. Unless otherwise stated, the boiling range distributions of crude oil feeds, total products, and / or crude oil products are determined by ASTM "D5307. "C5 asphaltene" refers to asphaltenes that are insoluble in pentane. The content of C5 asphaltenes is determined by ASTM method D2007. The term "X metal" refers to one or more metals in the χ table of the periodic table. Column of—or more than one metal—or more than one compound, which (D, corresponding party; number of the periodic table (for example, 1 to 12). For example, “the first, or more than one metal—or more than one compound. Brother X Xanfansu refers to one or more elements of the periodic table 帛 X only, 46 200532010 / or meaning: One or more elements of one or more elements of the Xth table in the X series corresponds to the number of columns in the periodic table: Mouth not 'its 1 s marriage; I ~ J master 18). For example, "Panfanfansu" refers to one or more compounds in the 15th of the periodic table or one or more of the 15th Yuanle table— 啖 多 啖 $ and / or the cyclic species. Apply for the standard ◎, the weight of the metal compound of the periodic table, the weight of the elements of the periodic table, the weight of the compound of the periodic table is calculated based on the weight of the metal or element:;锢 Medium II in the catalyst ::: Ϊ is 0.067 grams per gram of catalyst. ^ Weight "content" refers to the matrix expressed as a weight fraction based on the total weight of the matrix (for example, the percentage weight of crude oil Yili "Wtppm" refers to the parts per million by weight.) Into the "crude oil feed / total product mixture, the mixture to be obtained." "Contact with the catalyst during processing means that the boiling range is distributed at 〇. 1 〇1. At 204 MPa. (: Hydrocarbons between (400 F) and 343 C (650 ° F). Hefenbayiyiguandao contains I is determined by ASTM method D5307. "Heteroatom" refers to the oxygen contained in the molecular structure of smoke , Nitrogen, and / or sulfur. Heteroatom content is determined by ASTM method for E3δ5 of oxygen, D5762 of total gas, and D4294 of sulfur-like sulfur. "Total nitrogen test" refers to nitrogen compounds with _ less than 40. Test surface μ fermented mole (bn,) is determined by ASTM method D2896. Hydrogen, hydrogen and / or compounds and / or react in the presence of crude oil feed and catalyst in crude oil feed Compounds that provide hydrogen. 47 200532010 Estimates include, but are not limited to, hydrocarbons (for example, Clic4 hydrocarbons, such as Kobe 1 propane, Ding Huan, water, or mixtures thereof. May be performed; The amount of net nitrogen provided by the compound. "Basic crush strength" refers to the compressive force required to crush the catalyst. The crush strength is determined by ASTM method. Anti-private LHSV refers to the volume of liquid feed. Rate / total volume of catalyst, J k (hi) represents. The total volume of catalyst is calculated by summing the right media volume of the contact area. Those mentioned in the text.

"Liquid material" refers to-or more compounds that are liquid at standard temperature and pressure (re, 0 MPa, hereinafter referred to as "STP") ... and the product is "or liquid containing STP"- A composition of one or more compounds in combination with a solid state or more compounds under up. The Periodic Table 'refers to the periodic table specified by the International Union of Pure and Applied Chemistry (IUPAC) in November 2003. "Metals in the form of metal salts of organic acids refer to alkali metals, alkaline earth metals,

Zinc, arsenic, chromium, or a combination thereof. The metal content in the form of a metal salt of an organic acid was measured by the AS TM method D 1 3 1 8. The '' Micro Residual Carbon '("MCR") content refers to the amount of residual carbon left after the substrate is evaporated and pyrolyzed. The MCR content is measured by ASTM method D4530. Naphtha means a hydrocarbon component with a boiling range distribution between 38 ° C (100 F) and 200 C (3 92 ° F) at 0.1 MPa. The naphtha content is determined by ASTM method D5307.

Ni / V / Fe refers to recording, starvation, iron, or a combination thereof. "Ni / V / Fe content" refers to the content of nickel, vanadium, iron, or a combination thereof. 48 200532010 The mimic content is determined by the AS ™ method D5708. "―, Means the amount per cubic meter of crude oil feed. Standard stereo. "Non-carboxylic acid-containing organic oxygen compounds refer to organic oxygen compounds that do not contain a carboxyl group (-co2-). Non-slow-acid organic oxygen compounds include & _, Aldehyde 'or a combination thereof, which does not contain minus. Uncontrollable gas "means an A gaseous component and / or a mixture of these components under STP. The P (off / on) value or 'p value' refers to a value indicating the tendency of asphaltenes to flocculate in crude oil feed. The measurement of the p value is described by J.J. Heithaus in Chuan π⑽ / <

Measurement and Significance of Asphaltene by Institute of Petroleum ^ V〇l. 48? Number 458, February 19625 pp. 45-33

Peptization ', "pore size", "median pore size," and "pore volume" refer to the pore size, median pore size, and pore volume determined by the aSTM method D4284 (mercury porosity method with a contact angle of 140). A micromeritics® A9220 instrument (Micromeritics Inc., Norcross Georgia, U_S.A_) can be used to determine these values. ❿ "Residue" means a component with a boiling range distribution above 538 ° C (1000 T), such as the ASTM method Tested by D5307. "SCFB" refers to the standard cubic absorption of gas in the crude oil feed per barrel. The "surface area of the catalyst" is determined by ASTM method D3663. "TAN" means the total acid value, expressed as milligrams of OH ("mg") per gram ("g") of the sample. TAN is measured by ASTM method D664. "VGO" refers to hydrocarbons with a boiling range distribution between 343 ° C (650 49 200532010 卞) and 538 t (1000 τ) at 0.101 MPa. The VG0 content was measured by the astm method D5307. "Viscosity, refers to the dynamic viscosity at 37.8 t (100. Viscosity is measured using ASTM method D445. In the case of this application, it should be understood that if the properties of the tested substrate are obtained within the limits of the test method In addition, this test method can be modified and / or re-authorized to test such properties. Crude oil can be produced and / or carbonized from hydrocarbons containing structures and then stabilized. Crude oil can include crude oil. Crude oil is usually solid, Semi-solid, and :: liquid. Stabilization may include, but is not limited to, the removal of non-condensable gases, =, salts', or combinations thereof in crude oil to form stable crude oil. Such stabilization may typically occur at or near production And / or retorting sites. Stable crude oils are typically not prepared for multi-component distillation and / or fractionation, and have a multi-component distribution (such as naphtha, distillates, VG0, and / or lubricating oil). Including "… ... Tian Dizhu, but not limited to atmospheric distillation and / or reduced pressure distillation. Undistilled and / or unsecured stable crude oil may contain at least 0. per gram of crude oil Φ. 5 Μ to ... Brother crude oil Examples of 忐 9 stable knives with a stone anoresis number greater than 4 include all crude oils, knives ^ ^ t ", Yu crude oil, desalted crude oil, de-Bg Yu surplus crude oil, or a combination thereof." 朱 余 脱1 At least part of the ingredients with Buddha's point at 0101 and 1 atm at 95 卞 have been privately removed. Typical 'C (with a maximum content of ° in crude oil: the remaining crude oil is distilled per gram.-Gram of this type of ingredient .. ~ °°. 5 grams' or at most dry L 疋 crude oil has the property of allowing stable crude oil to be transported to conventional processing equipment by means of a shipping vehicle (eg 50 200532010 pipeline, truck, or ship). Others the crude oil so that they have one or more undesirable properties inappropriate ', ..., $ shell Kaibara> for the purposes of the delivery vehicle and / or the processing device may not be acceptable,, -. a drink and, therefore Fu

Low economic value of crude oil. This economic value may be as expensive as the production, transportation, and / or treatment of the valley state of eight inferior crude oils. The nature of inferior crude oils may include, but is not limited to: a) a TAN of at least 0 and less than 0.3; b ) A viscosity of at least 10 cSt; c) a specific gravity of at most ^, d) a total Nl / V / Fe content of at least 20000 g or at least 0.00 000 g of Ni / V per gram of crude oil / Fe; e) total heteroatom content is at least 0.005 grams of heteroatoms per gram of crude oil; f) residue content is at least 0.01 grams of residues per gram of crude oil; g) Cs asphaltene content is per gram of crude oil At least 0.04 grams of I asphaltene; h) an MCR content of at least 0.002 grams of MCR per gram of crude oil; i) an organic acid metal salt in the form of a metal content of at least 0.00001 grams of metal per gram of crude oil; or] ·) Its combination. 2 In several specific examples, inferior crude oil may contain at least 0.2 grams of residues, at least 0.3 grams of residues, at least 0.5 grams of residues, or at least 0.9 grams of residues per gram of inferior crude oil. Thing. In some specific examples, the inferior element may have a TAN 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 specific examples, inferior crude oil may have a sulfur content of at least 0.0005 grams, at least 0.001 grams, or at least 0.02 grams per gram of inferior crude oil. In several specific examples, inferior crude oil has properties including, but not limited to: a) a TAN of at least 0.5; b) an oxygen content of at least 0.005 grams of oxygen per gram of crude oil feed; c) Cs asphaltenes The content is at least 0.04 grams of C5 asphaltene per gram of crude oil feed 51 200532010 with a API with a specific gravity of at least 10 ::: viscosity (e.g., the feed is from the feed to> 10 cSt) * The metal content in the form of a metal salt of an organic acid is at least 0.00001 g of metal in each of the von mother grams of crude oil; or f) a combination thereof. Inferior crude oil can be inferred per gram of inferior crude oil. Τ j a 3 · At least 0 001 grams, at least 0.005 grams, or at least 0.01 grams of boiling. Where I Niyawang knife cloth at 0.101 MPa

Hydrocarbons between 90 C and 200 ° C; a boiling range distribution of at least 0.001 g, at least 0.05 g, or at least 0.001 g between 2000 and 0.0001 MPa. Hydrocarbons between 0 ° C and 300 ° C; hydrocarbons with a boiling range distribution of at least 0.001 g, at least 0.05 g, or at least 0.001 g between 300 ° C and 40 ° C at 0.101 MPa; And at least 0.001 grams, at least 0.005 grams, or at least 0.001 grams of hydrocarbons with a boiling range distribution between 0.1 ° C and 650 ° C at 0.101 MPa. Inferior crude oil may contain at least 0.001 per gram of inferior crude oil Grams, at least 0.005 grams, or at least 0.01 grams of boiling range distribution at o.ioi MPa

Hydrocarbons up to 100 ° C; at least 0.001 grams, at least 0.005 grams, or at least 0.001 grams of hydrocarbons with a boiling range distribution between 0.1 ° C and 200 ° C at 0.11 MPa; at least 0.001 Grams, at least 0.005 grams, or at least 0.001 grams of hydrocarbons with a boiling range distribution between 200 ° C and 300 ° C at 0.101 MPa; at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams boiling range distribution of hydrocarbons between 30 ° C and 400 ° C at 0.101 MPa; and at least 0.001 grams, at least 0.005 grams, or at least 0.001 grams boiling range distribution Hydrocarbons between 400 ° C and 650 ° C at 0 · 101 MPa. In addition to the higher boiling point components, several inferior crudes may contain at least 0.001 g, at least 0 per gram of inferior crude. · 005 grams, or at least 0. 01 52 200532010 grams of hydrocarbons with a boiling range distribution of up to 100 ° C at 0.101 MPa. Typically, inferior crude oil has a maximum of 0.2 grams or a maximum of 0.1 per gram of inferior crude oil. The content of such hydrocarbons in grams. Several inferior crude oils may contain at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of boiling range distribution below 0.101 MPa per gram of inferior crude oil. Smoke at 200 ° C. Several inferior crude oils may contain at least 0.001 grams of at least 0.005 grams per gram of inferior crude oil, or at least 0.01 grams of hydrocarbons having a boiling range distribution of at least 650 ° C. The methods described herein may be used Examples of inferior crudes processed include, but are not limited to, crudes from the following regions of the world: US Gulf Coast and southern California, Canada Tar sands, Brazilian Santos and Campos basins, Egyptian Gulf of Suez, Chad, United Kingdom North Sea, Angola Offshore, Chinese Bohai Bay, Venezuelan Zulia, Malaysia, and Indonesia Sumatra. Dealing with inferior crude oil can enhance the properties of inferior crude oil so that the crude oil can be accepted for transportation and / or processing. The crude oil and / or inferior crude oil to be processed herein is referred to as "" Crude feed, This crude feed can be a distillate as described herein. Crude products obtained from processing a crude feed as described herein are generally suitable for transportation and / or processing. As described herein The properties of the produced crude oil products are closer to the corresponding properties of West Texas Intermediate crude oil than crude oil feed, or Closer to the corresponding properties of Brent (Brent) crude oil, thereby increasing the economic value of the crude feed. This type of crude oil product can be refined with little or no pretreatment, thereby increasing the amount of 53 200532010 $ to the staff. Treatment can include desulfurization, demetallization and / or atmospheric distillation to remove impurities. 'Processing a crude oil feed in accordance with the present invention may include contacting the crude oil feed with a catalyst in a contact zone and / or a combination of two or more contact zones. In the contact zone, at least one property of the oil feed may be changed compared to the same property of the crude feed by contacting the crude feed with one or more catalysts. In several examples, the contact was performed in the presence of a hydrogen source. In several specific examples, the lice source provides a relatively small amount of hydrogen-or hydrocarbons to crude oil in order to react under specific exposure conditions. ° Figure 1 is a simplified diagram of a contact system 100, which includes a contact area 102. The crude oil feed enters the contact zone 102 via a conduit 104. The contact area may be an anti-cry, a part of a reactor, multiple parts of a reactor, or a combination thereof. Contact zone: Examples include stacked-bed reactors, fixed-bed reactors, 反应 bed reactors, ㈣ stirred tank reactors, ⑺Ca ”, fluidized bed reactions ^ spray reactions Z ′, and liquid / liquid contactors. In a specific embodiment, the contact system is located or connected to offshore equipment. In the contact system 100, the contact of the crude oil feed with the catalyst may be a continuous or batch process. This contact zone may contain one or more catalysts (eg Two catalysts). In several specific examples, the contact of the crude oil feed with the first catalyst of the two catalysts can reduce the crude oil feed into the TAN. The crude oil feed that has been reduced with the TAN and the first catalyst Subsequent contact is to reduce the heteroatom content and increase the specific gravity of the API. In other specific shots, after the crude oil is contacted with-or more catalysts, the TAN, viscosity, Nl / V / Fe content, heteroatom content, and residue of the crude oil feed Material content, API specific gravity, or a combination of these properties will change by at least 10% compared to the same properties of the crude oil feed 54 200532010. In certain specific examples, the contact (the contact media in I is between 10 and 60 months). Ugly product / 〇 '2G to 50% by volume, 3 () to 4Q% by volume of the total volume of crude oil feed in the contact zone. In some specific examples, the slurry of catalyst and crude oil feed may be included in each 100 grams of crude oil feed in the contact zone. Gu Ke 0.005 to 5 grams, or 0.01 to 3 grams of catalyst. The contact conditions in the dead zone may include, but are not limited to, temperature, pressure, hydrogen source flow, crude oil feed flow ', or a combination thereof. Control the contact conditions in several specific examples to produce characteristic crude oil products. The connection can be distributed in the range of 50 to 60, 60 to gift, 70 to _, or 80 to 42 C. The contact area The pressure can be distributed in the range of (M to 20MPa '; Erca' 4 to 10 cents or 6 to 8). Crude oil is imported, and the LHSV is usually distributed in the range of 0.1 to 3011-1, 0.5 to 2511-1 '1 to 20, LHSV 15 wide,' or 2 to 10 h 1 range. In some specific examples, LHSV is at least 5 h-1, at least! J 1, $ 丨 at least 2 0h 'to ^ is Old, at least 15h ·, or in specific examples where the hydrogen source is supplied as a gas (such as hydrogen), the ratio of gaseous hydrogen = original: 5 feed is typically distributed in ... Wide °, _ _, 1 to 8, _ Nm, 3, 2 to English, to 3,000 NmVm3 'or 10 to 800 Nm3 / m3 spot catalyst and It': Hydrogen is derived from several specific examples in combination with a carrier gas And == over-contact zone. The carrier gas can be, for example, nitrogen, gas, and / or airborne milk can promote the flow of crude oil feed in the zone of contact. The carrier gas can also increase the amount of 5 in the zone of contact. In some specific cases, the source of argon (such as hydrogen, methane or ethane) can be used as a carrier gas and recycled through the contact zone. The lice source may enter the contact zone 102 in parallel with the crude oil feed in the conduit 104 or via the conduit 106, respectively. In the contact zone 10 ", the contact system of the crude oil feed with the catalyst produces a total product containing crude oil products, and in some specific examples gas. In several specific examples, the carrier gas system and the crude oil feed or at V s 1 Combined with a hydrogen source in 06. The total product can leave the contact zone 1 and enter the separation zone 108 via the conduit 110.

In the separation zone 108, crude oil products and gases can be separated from the total product using generally known inseparable techniques, such as gas-liquid separation. Crude oil products may be separated by conduit U2 and separated by 108, and transported to transportation carriers, pipelines, storage containers, refineries, other processing areas, or a combination thereof. Gases may include gases generated during the process (such as hydrogen sulfide, carbon dioxide, and / or nitric oxide, excess gaseous hydrogen sources, and / or carrier gas. Excess gas may be re-ridden until contact with the system, can be purified, transported To other processing zones, storage containers, or a combination thereof. In several specific examples, the product is produced in two or more crude oil products and gases. 'Contacting the crude feed with the catalyst to produce a total contact zone can be performed. Isolate the total product to

Figures 2 to 3 contain two or two marriage techniques

Contact system for flying contact area 1 0C

A simplified diagram of a specific example. As shown in FIG. 2A :) In R A and 2B, the contact system 100 includes the contact areas 102 and 114. Figures 3A and 3B. Contact areas 102, 1 14, 11 In Figures 2A and 3A, the 'contact area 102' is depicted as individual contact areas in the reactor. Eyebrows and crude oil are fed into the area 102 through the conduit 1 04 to 7 56 200532010. In several specific examples, the 'carrying gas cut f 1 () 6 towel stands with the gas source and is introduced into the contact area as a mixture. In certain specific examples, as shown in Figs. 3 and 3B, the gas source and / or carrier gas can be passed through the "H) 6 and / or via the conduit 1Q6, in the opposite direction of the crude oil feed flow, the fish crude oil feed Distributor—or multiple contact zones. Reverse flow of crude oil feed = Addition of hydrogen source and / or carrier gas can promote crude oil feed with catalyst or contact. 〇 and / In contact with H 102 towels, crude oil feed and The contact of the catalyst will generate raw materials ^ This raw material stream flows from the contact angle ㈣102 to the contact zone ιΐ 4. In Figure 3B, the raw material stream flows from the contact zone U4 to the contact zone H6. A contact zone 102, 114, 116 may include _ Or multiple catalysts. As shown in the figure, the 'raw material flow leaves the receiving area 102 through the guide t 118 and enters the area m. As shown in FIG. 3B' the raw material flow leaves the contact area 1 14 through the conduit 8 and enters the contact. Zone 丨 丨 6. The raw material stream may be in additional contact with the contact zone 114 and / or the contact zone 116 to generate a total product. The total product leaves the contact zone 114 and / or the contact zone 进 enters the separation zone 1G8 via a conduit no. Crude product And / or the gas system is separated from the total product. The crude product leaves the separation zone 108 via a conduit 112. Fig. 4 is a simplified diagram of a specific example of the separation zone upstream of the contact system 。. Inferior crude oil (distilled or non-distilled) is introduced into the separation zone 120 via the conduit 122. In the separation zone ΐ2Φ ,: τ, Π to乂 A part of the inferior crude oil is separated using a technique known in the technology (such as Hebu, membrane separation, and decompression) to produce crude oil feed. For example, + cattle W and 3, water can be At least partly from inferior crude oil 57 200532010

from. In another example, a knife having a boiling range distribution below 951 or below 10 ° C can be at least partially separated from inferior crude oil to produce a crude feed. In several specific examples, at least a portion of naphtha And compounds that are more volatile than naphtha are separated from inferior crude oil. In some specific examples, at least a portion of the separated components leave the separation zone 120 via the conduit 124.

The crude oil feed obtained from the separation zone 120 is, in some embodiments, a mixture of components having a boiling range distribution of at least $ 10 (rc, or in some embodiments, the boiling range knife cloth to 120 c. Typical. In terms of separation, the separated crude oil feed comprises a mixture of components having a boiling range distribution of 100 to 1000 OC, 120 to 900 C, or 200 to 800 t. At least a portion of the crude oil feed leaves via conduit 126 The separation zone 120 enters the contact system (see the contact zone in Figures 1 to 3) for further processing to produce crude oil products. In several specific examples, the separation zone 120 may be located upstream or downstream of the desalination unit. After the treatment, the crude oil product is Exit the contact system 100 via a conduit " 2. In several specific examples, the crude oil product is blended with the same or the same oil as the crude oil feed. For example, the crude oil product can be combined with crude oil having different viscosities. A blended product having a viscosity between the viscosity of the crude product and the degree of origin is produced. In another example, the crude product may be blended with raw materials and oils with different TANs, thereby producing a product having a viscosity between Produce Between the product and the crude TAN. This blended product may be suitable and / or processed. '

As shown in FIG. 5, 104 enters the contact system in a specific embodiment, and the crude oil feed is via system 100, and at least a part of the crude product is guided by 58 200532010, and the director 128 leaves the contact system 100 and is introduced into the blending zone 13. . In the blending zone, at least a portion of the crude oil product is combined with one or more industrial production streams (eg, hydrocarbon streams such as naphtha produced by separating one or more crude feeds), crude oil, crude feeds, or The mixtures are combined to produce a blended product. Industrial production streams, crude feeds, crude oil, or mixtures thereof are directed via conduit 132 into blending zone 130 or upstream of such blending zone. The mixing system may be located at or near the blending zone 130. The blended product can meet the product specifications specified by the refinery and / or conveyor. Product specifications include, but are not limited to, Αρι specific gravity, ταν,

Viscosity, or range or limit of combinations. The blended product leaves the blending zone 1 30 for delivery or processing via a catheter ##. In FIG. 6, the inferior crude oil is introduced into the separation zone through the conduit 122, and the inferior crude oil is separated to generate a crude oil feed as previously described. The crude oil feed then enters the contact system 100 through the guide fm. At least some of the components of the inferior crude oil leave the separation zone 120 via the conduit 124. At least a portion of the crude oil product exits the contact system 100 via the conduit 128 and enters the blending zone. Other industrial production streams and / or crude oil enter the blending directly or via the conduit 132.

The combined zone 130 is combined with the crude product to produce a blended product. The blended product exits the blended zone 130 via a conduit 134. In some specific examples, crude oil products and / or push products are delivered to refineries and / or processing equipment. Crude products and / or blended products can be processed to produce industrial products, such as transportation fuels, heating fuels, skimmers or chemicals. Processing may include distilling and / or fractionating the crude product and / or blending the product to produce more than one crane fraction. In several specific examples, crude products, push products, and / or multiple fractions may be hydrotreated. ′ 59 200532010 In several specific examples, the crude oil product has a TAN of up to 90%, up to 鄕, up to 30%, or up to & 10% of the TAN of the crude oil feed. In several specific examples, the 'crude product' has To 80%, ^ to 70% ′ 30 to 60%, or within 50% of the TAN of the crude oil feed. In certain specific examples, the crude oil product has a TAN of at most 0.5, at most 0.3, at most 02, at most 01, or at most 0.05. The TAN of the crude product is usually at least 0. More commonly, 'is at least G.GG1. In several specific examples, the tan of the crude product can be in the range of 0.001 to 0.5, 0.001 to 0.02, or 005 to 0 ".

In some specific examples, crude oil products have a total Ni / V / Fe content of 90%, 5G% at most, 1 ()% at most, Ni / Vout at most, or 3% of crude oil feed. V / Fe content. This crude oil product has a total Ni / V / Fe content of 1 to 80%, 10 to 70%, and 20% in several slaves.

To 60%, or 30 to 50% of the Ni / V / Fe content of the crude feed. In a specific embodiment, the crude oil product has from 1x grams to 5 X 10 grams' 3 x 10-7 grams to 2 X ι05 grams per gram of crude oil product, or 1 X 106 grams to 1 X Total Ni / v / Fe content in the range of 10-5 grams. In a specific embodiment ::, this crude oil contains up to 2 x 10.5 g of Ni / V / Fe. In several months and by way of example only, the total Ni / V / Fe content of the crude product is 70 to 120% or 90 to 10% of the Ni / v / Fe content of the crude feed. In some examples, the total content of metals in the form of organic acid metal salt in crude oil products is the most & column%, the maximum is 5G%, the maximum is 10%, or = 5% of the original "Organic from feed Total metal content in the form of an acid metal salt. In the case of κ, the crude oil product has the form of a metal salt of organic acid 60 200532010 The total content is 1 to 80% '10 to 70% 20 to 60%' or 30 to 50% of the crude oil feed The total metal content in the form of a metal salt of an organic acid. Organic acids commonly used to form metal salts include, but are not limited to, carboxylic acids, thiols, imines, sulfonic acids, and sulfonates. Examples of carboxylic acids include, but are not limited to, naphthenic acid, phenanthronic acid, and phenylarsinic acid. The metal part of the metal salt may include alkali metals (such as lithium, sodium, and potassium), alkaline earth metals (such as magnesium, calcium, and barium), metals (such as zinc and money), and metals (such as zinc) , Column 6 metals (such as chromium), or mixtures thereof.

~ In the specific examples, the total content of the metal in the form of organic acid metal salt per gram of crude oil product is from 0,001 grams to 00005 grams, and 0000Q003 grams to 0,000 grams per gram of crude oil products. 1 gram to 0.000 gram of metal in the form of a metal salt of an organic acid: In the specific example of the right-hand dry wall, the total metal content of the metal salt of the organic acid in the crude product is 70 to 13%, 8 To 120%, or 90% to the total metal content of organic acid metal salt in the crude oil feed. Contact: In the specific example of the specific example, ’crude oil feed and catalyst under contact conditions:

^ The API gravity of the crude product produced is 70 to i3Q%, 80i20 / 〇, 90 to 110%, or 100-

API 1 of King 1's crude oil feed: In a specific embodiment, crude oil product 1… or 16 to 25. ^ 4 14 ^ 40 In certain specific examples, 5 <at most f ^. / ^,, / / Have a viscosity of up to 90%, evening is 80 / 〇, or up to $ 70%

In the physical example, 5a d, the viscosity of the department. In some J or 〇Γ objects have viscosity in the heart sail, 2 () to 50%, 30 to the crude oil feed dry. In some specific examples, 61 200532010, the stickiness of crude oil products, ^ #From the viscosity of 90% of the crude oil feed, the API proportion of this crude product on the same day was 7G, and the crude oil feed was 2%. The specific gravity of Aρι. Or if it is a specific example, the crude oil product has the largest total heteroatom content, at most, or a maximum of 5% of the atomic total crude heteroatom content of the crude oil feed: in a specific embodiment, the crude oil product has at least Among them, at least: 3 °%, at least 80%, or κ 4 proton, from the total content of heteroatoms. In some specific examples, the crude oil production is 90%, and the maximum is 50%. The crude oil product at Shengxi is 10%, or at most 5%, at least 30%, until the crude oil product has a sulfur content of at least 80%, or at least a Q () 0 / Sulfur content. In a few Gezhi "quote is 99 /. Crude oil 70 to 130. / qa — In 1j, the sulfur content of crude oil products is the sulfur content. The crude oil feed from 1 to U0 / ❹ is included in several specific examples, 900 /,-^^, and the total nitrogen content of the oil product may be up to 90 /. The maximum nitrogen content is 80% and the maximum is 10%. In a specific system; take the crude oil feed ^ f, 5%, in the monthly example, the crude oil product has a content of at least 1%, at least 30%, at least 800 //, The total nitrogen content of the crude oil feed in Xin 3 nitrogen. Or at least 99%. In some specific examples, the crude oil product is 95%, the maximum is ㈣, the maximum is Λ, 0 / ^ ^ is 50 / 〇, and the attack is】 0%, or the most. Dagger 5 /. The chlorine content of the crude oil feed. Take: ㈣ Have a test nitrogen content to, at least two less than the original 200532010 80%, or at least the basic nitrogen content of crude oil feed. Gray right dry concrete example is 90%, the maximum is 50%. The oxygen content of a product may be at most °, which is 30% at most, and at most lf) 0 /, formula #xiyan 5% crude oil feed 4 10 /. , Or take as much as having at least oxygen content. In the specific example of the shirt, the crude oil product has an oxygen content of 99%, at least 30%, at least 80%, or at least yy / 0 of the crude oil feed. The oxygen content in ... The crude oil production of the dove of crude oil contains! ^ G to 7G%, 2G to 6G%, or 30 to

..,. Within range. In some specific examples, the carboxylic acid compound of the crude oil product is 50%, up to 10%, or up to 3: 9%, up to the material content. In the crude oil feed in a specific form ^ / The phosphonate compound content is at least "/ 5 crude oil products with total acid compounds", 0 ^ is 30%, at least 80%, or at least 99% of the total carboxylic acid compound content in the crude feed.

In several specific examples, selected organic oxygen compounds in a crude oil feed can be reduced. In several specific examples, the _ and / or _ metal salt may be chemically reduced before the non-carboxylic acid-containing organic oxygen compound. Organic oxygen compounds containing carboxylic acids and non-carboxylic acids in crude oil products can be identified by analyzing the crude oil products using generally known spectroscopic methods (e.g., infrared analysis, mass spectrometry ', and / or gas chromatography). This crude oil product has a specific oxygen content of φ 1 in the bamboo case. It has an oxygen content of at most 90% 'and a maximum of 8G%. The TAN of this crude oil product is at most 90%, at most 70%, at most 50%, or at most 40% of the crude oil feed Ding Ba / In a specific embodiment, the crude product has an oxygen content of at least ι% , At least 63 200532010 is 30% 'at least 80%, or at least the oxygen content of the crude oil feed, and this crude oil product has a TAN of at least $ ι%, at least, at least 80/0 or The TAN of the crude oil feed is at least 99/0. In addition, crude oil products may have a carboxylic acid and / or metal carboxylic acid salt content of up to 90%, up to 70%, up to 50%, or up to 40/03 non-carboxylic organic oxygen compounds in the crude feed. The content is between 70 and 130. /. , 80 to 120%, or 90 to 110% of the crude oil feed contains non-carboxylic acid organic oxides. In the specific example of the right stem, the crude oil product contained in its molecular structure 0.05 to 0.15 g or 009 to 013 g of hydrogen per gram of crude oil product. This crude oil product may contain, in its molecular structure, 0.8 to 0.9 grams or U2i of 0.88 grams of carbon per gram of crude product. The atomic nitrogen to atomic carbon ratio (H / C) of the crude oil product may be in the range of 70 to 130%, 80 to 120%, or 90 to 110% of the atomic H / C ratio of the crude oil feed. The atomic H / c ratio of the crude oil product in the range of 10 to 30% of the atomic H / C ratio of the crude oil feed shows that relatively little hydrogen is absorbed and / or consumed during overworking, and / or Hydrogen-based on-site production. · Crude oil products contain components in a range of boiling points. In several specific examples, the 'crude oil product contains per gram of crude oil product: at least 0.0001 g, or a boiling range distribution of 0.001 to 0.5 g, and at most ^ its k, at least 0.001 g, or 〇01 ～ 05 grams of boiling range distribution at 010 MPa; 丨 hydrocarbons between 〇OOc and 200C; at least 0001 grams, or 0001 to 〇5 grams of boiling range distribution at 〇ι Hydrocarbons between 〇 (Γ (: and 300t :) at 〇1 MPa; at least 0.001 g, or 0.001 to 0.05 g boiling range distribution at 001 64 200532010 MPa Hydrocarbons between 300 ° C and 400 ° C; and hydrocarbons with a boiling range of at least 0.001 g, or 0.001 to 0.5 g, distributed between 400 ° C and 538 ° C at o.ioi MPa. In a specific example, the crude oil product contains at least 0.001 grams of boiling range distribution per gram of crude oil product, hydrocarbons of up to 100 ° C at 0.101 MPa and / or at least 0.001 grams of boiling range distribution between 0.101 MPa Hydrocarbons between 100 ° C and 200 ° C.

In several specific examples, the crude product may contain at least 0.001 grams, or at least 0.01 grams of naphtha per gram of crude product. In other specific examples, the crude product may have a naphtha content of up to 0.6 g, or up to 0.8 g, per gram of crude product. ν / Gong · Xiao acupoint cleverly, swordsmanship 7 篁 130〇 /. '80 to 120%, or 90 to 11% of the crude oil feed fraction content Crude oil fraction content per gram of crude oil product can be between 0 00_ to (g, 0.001 to 0.3 g, or 0.002 g to In the specific embodiment, the crude product has a VG content of%

V% of the crude oil feed at r%, 8G to 8g, or 9G to UG% ^ In the W example, the crude oil product is in the range of _ to ㈣ grams per gram, or 0.002 to 22 0.001 to 0.3 grams VG0 content within. In several specific examples, the crude oil product has ⑽, 叫 or 9. to :? Here is ... This eyebrow, A $ μ 1 ^ ^ Residues of crude oil Dakota 4 = This crude oil product can have 0_ grams to 0.5 grams per gram of crude oil product, and _ to 〇. Where υ.οοι to 〇3 grams , 65 200532010 A residual content in the range of 0.005 to 0.2 g, or 0.001 to 0.001 g. · In the specific examples of known crude oil products, the crude oil product has an MCR content of 70 to 130%, 80 to 120%, or 90 to 110% of the crude oil feed, and the crude product has a q asphaltene content Up to 90%, up to 80% ', or up to 5G% of crude oil feed ~ Alexandrite content. In specific examples, the C5 asphaltene content of the crude oil feed is at least 10%, at least 60% ', or at least &amp; 70% of the Cs cyanocyanine content of the crude oil feed, and at the same time, the MCR content of the oil product Within the range of 10 to 30% of the mcr content of crude oil feed. In several specific examples, reducing the q-leaching cyanide content of the crude oil feed while maintaining a relatively stable MCR content can increase the stability of the crude oil feed / total product mixture. In the specific example of the right stem, the mathematical relationship between the Cs asphaltene content and the mcr content can be used to generate the viscosity component of the crude oil feed compared to the degree component of the crude oil product. For example, the sum of the q cyanide content of the crude feed and the MCR content of the crude feed can be expressed as S. The sum of the C5 cyanocyanine content of the crude oil product and the mcr content of the crude oil product can be expressed as a comparison of these sums (s, and s) to estimate the net reduction in high viscosity components in the crude oil feed. To 99%, 10 to 90%, or 20 to S. In some specific examples, the ratio of the mcr content to the C5 asphaltene content of the crude product is in the range of 10 to 3.0, 1.2 to 20, or 1.3 to 1.9. In the specific examples of formulas and formulas, crude oil products have a maximum MCR content of at most 80%, at most 50%, or at most 10% of the crude feed. In several specific examples, the crude oil product has an MCR content of 66 200532010 ranging from 1 to 80%, 10 to 70% ′ 20 to 60%, or 30 to 50% of the MCR content of the crude oil feed. The crude oil product contains 0.0001 to (M grams, 0.05 to 0.005 grams, or 0.01 to 0.05 grams of MCR per gram of crude oil product in several examples. In several specific examples, the crude oil product is present in each gram. Crude products contain more than 0 grams, but less than 0.01 grams, 0.00001 to 0.001 grams, or 0.0000 to 0.0001 grams of total catalyst. The catalyst can help stabilize the crude product during transportation and / or processing. Catalyst Can inhibit corrosion, inhibit friction, and / or increase the water-separation capacity of crude oil products. The methods described herein can be configured to add one or more of the catalysts described herein to crude oil products during household management. Contact The crude oil product produced by the system 1000 contact has different properties from the original and feed properties. Such properties can include, but are not limited to: a) reduced TAN; b) reduced viscosity; c) reduced total Ni / V / Fe content; d) reduced sulfur, oxygen, nitrogen, or a combination thereof; e) reduced residue content; 0 reduced asphaltene content; g) reduced MCR content; h) API weight ; I) Reduced metal content of organic acid metal salt form 戍 J) Its combination. In several specific examples, one or more properties of the crude product may be selectively changed compared to the crude feed, while other properties are not changed as much or substantially unchanged. For example, it may be desirable to selectively reduce only the TAN in a crude oil feed without significantly altering the amount of other components such as sulfur, residues, Nl / V / Fe, or VGO. In this way, the hydrogen uptake during the contact can be "concentrated" according to the decrease in TAN without affecting the reduction of other components. Therefore, although less hydrogen is used, the TAN of the crude oil feed can still be reduced , Because a smaller amount of this hydrogen will also be used to reduce other components in the crude oil feed. 67 200532010. For example, if inferior crude oil has a high TAN 'but the sulfur content is within the processing and / or transportation specifications Recipients, this type of crude feed can be processed more efficiently to reduce TAN without also reducing sulfur. The catalyst used in one or more embodiments of the present invention may include one or more bulk metals and / or One or more metals on the carrier. The metal can be in the form of an element or a metal compound. The catalyst described herein can be introduced into the contact zone as a precursor, and then becomes an active catalyst in the contact zone (for example, and (When the sulfur and / or sulfur-containing crude feed is in contact with the precursor). The catalyst or catalyst combination used as described herein may or may not be a commodity catalyst. It covers the commodities used in the description Examples of catalysts include HDS3; HDS22; HDN60; C234; C31 1; C344; C411; C424; C344; C444; C447; C454; C448; C524; C534; DN110; DN120; DN130; DN140; DN190; DN200; DN800; DN800; DN800; DN2318 DN3100; DN3110; DN3300; DN3310; RC400; RC410 RN412; RN400; RN420; RN440; RN450; RN650; RN5210 RN5610; RN5650; RM430; RM5030; Z763; Z603753; Z603713; Z603753; Z603753; Z603753; Z603673; Z603753 It can be obtained from CRI International, Inc. (Houston, Texas, USA). In several specific examples, the catalyst used to change the properties of the crude oil feed comprises one or more metals 5 to 10 on the carrier. Columns 5 to 10 include, but are not limited to, chrome, molybdenum, rhenium, fierce, erroneous, baht, iron, starting, recording, ruthenium, Ιε, thorium, iron, watch, iron, or mixtures thereof. Each gram of the catalyst may have at least 0.0001 grams, at least 0_001 grams, at least 0.01 200532010 grams, or in the range of 0.0001 to n AA ^ ancient, urn 6 grams, 0.005 to 0.3 grams, 〇_ to (M grams or · 〇 ～ 〇〇〇〇〇〇〇〇〇〇〇〇〇〇。 Total metal content in metal ◦ In some specific examples, the catalyst except τ 坌 flute—this series except for 5 to 10 metal In addition, it contains 15 columns. The element of the 15th column is "bei dagger". The catalyst may have a total content of 15 5% of the element. Jinyou Gray Guli in the mother gram catalyst is 0.000001 to 0.1 g, 0.00001 to 0.06 g, 〇〇〇〇〇〇 Wang υ · ϋ 3 grams 'or 0.001 to 001 grams in the range. In the specific example of the catalyst' catalyst contains the sixth metal. The catalyst

The master gram catalyst may have at least 0 0001 grams, at least 0.001 grams, at least ^^ and / or between .0 to 0.6 grams, from 0.001 to 〇3 grams, and from 005 to 0— 0.01 to 0.08 grams of total 6th metal. In several examples, the 'catalyst contains from 0.00001 to 0.006 grams of metal in each gram of catalyst. In some specific financial matters, in addition to the metal in column 6, it also contains Column 15 element.

. In the specific example of the one side, the right side, the catalyst includes a combination of the sixth metal and the fifth column and / or the seventh to the first G-metal. The molar ratios of the metal in the sixth column and the metal in the second column may be in the range of 0 to 20, i to 10, or 2 to $. In the range of 0.1 to 1, 1 t 10, or 2 to 5. In some specific examples, the catalyst includes the 15th element in addition to the 6th metal and the 5th and / or one or more metal spoons in the 7th to 10th columns, and 3. In other specific examples, the catalyst includes a G6 column metal and a 10th metal. The molar ratio of the total amount of metal in column 10 to the total amount of metal in column 6 in the catalyst can be in the range of 1 to 10, or 2 to 5. In a specific embodiment, the catalyst includes the fifth column of metal and the second column of metal. The molar ratio of the total amount of the 10th metal to the total amount of the 5th metal in the catalyst can be in the range of 1 to 10, or 2 to 5. In some specific real money, the metals in columns 5 to 1G are merged or deposited on a carrier to form a catalyst. In some specific examples, the combination of the 5th metal and the 15th column element is incorporated or deposited on a carrier to form a catalyst. In the specific example of metal and / or element loading, the weight of the catalyst includes all carriers, all metals and all elements. The support may be porous and may include a refractory oxide, a porous carbon-based material, a zeolite, or a combination thereof. Refractory oxides can include, but are not limited to, aluminum oxide, silicon oxide, aluminum oxide, titanium oxide, hafnium oxide, magnesium oxide, or mixtures thereof. The support may be obtained from an industrial manufacturer, such as Criterion Catalysts, "hn〇10 Fine LP (Houston, Texas, us. A). Porous carbon-based materials include, but are not limited to, activated carbon and / or terracotta graphite. Examples of zeolites include zeolite 1 fused, mercerized zeolite, ZSM-5 zeolite, and zeolite. Zeolites are available from industrial clothing manufacturers, such as Zeolyst (Valley Forge, Bu Jia Qiao Bu υ $ a ) 〇. In several specific examples, the carrier is prepared so that the carrier has an average pore size of at least 150 A, at least 170 A ', or at least 18 A. In specific embodiments, the' carrier is formed by water forming the carrier. The slurry is prepared. In several 2-body examples, acid is added to the slurry to promote the extrusion of the slurry: the acid is added in the required amount and by the required method to extrude the slurry in 2 releases. Desirable consistency. Examples of acids include, but are not limited to, nitric acid, sulfuric acid, and hydrochloric acid. Paper and slurry can be cut out and reported using commonly known catalyst extrusion methods and catalysts. Forms an extrudate. The extrudate can be in the range of 5 to 2 or 85 70 200532010 ± 5 C Heat treatment at a temperature-for a period of time (for example, 0.5 to 8 small day guards) and / or until the humidity of the extrudate reaches the desired value. 孰 processed dials can be in _ to 1 fan. 〇 or _ more ' Further heat treatment is performed at a temperature in the range of I to form a support having an average pore size of at least 150. Ute, in specific examples, the support includes gamma oxide, tritium oxide, § alumina (X emulsified aluminum 'or its Mixtures. The amount of gamma alumina, delta alumina, alpha alumina 'or mixtures thereof may be between 0.0001 and 0.99 grams per gram of catalyst support, and between 0.001 and 0.5 grams, and 0.015 grams per year. • Within the range of gram, or up to 0.1 gram, it is determined by X-ray diffraction. In some specific examples, the carrier contains alone or in combination with other forms of oxide, and the content of θ oxide is in per gram of body. 0.1 to 0.99 grams, 0.5 to 0.9 grams, or 0.6 to 0.8 grams within the dry range 'which is borrowed from X-ray diffraction. In specific examples of the material, the carrier may contain at least GU, at least G. 3 grams, at least ⑴ ... or at least 0 8 grams of Θ alumina, which is determined by X-ray diffraction. -Generally known catalyst preparation techniques. Examples of catalyst preparation methods are described in U.S. Patent No. f 6,21 8,333 issued to GabdelQv et al .; ; 5,744, G25 awarded to the Temple Temple, and US Patent Application Publication No. 20030111391 issued to Bhan.… In several specific examples, the carrier can be impregnated with metal to form a catalyst. In specific specific examples, in Before the metal is impregnated, the carrier is ordered at a temperature ranging from c ′ 450 to 1000 t ′ or 600 to 900 t, and 4 is processed. In several specific examples, the impregnation aid can be used during the preparation of the catalyst 71 200532010. Examples of the impregnation aid include a citric acid component, ethylenediaminetetraacetic acid (EDTA), ammonia, or a mixture thereof.

In a specific embodiment, the catalyst may be formed by adding or mixing columns 5 to 10 of the metal into a heat-treated formed carrier mixture ("cover,"). The top surface of the heat-treated formed carrier is covered with metal to form Metals with a substantially or relatively uniform concentration usually give the catalyst favorable catalytic properties. Heat treating the formed support after each coating of the metal tends to improve the catalytic activity of the catalyst. The method of preparing the catalyst by the coating method is described in the description In U.S. Patent Application Publication No. 20031 1 1391 issued to Bhan. The 5th to 10th metal and carrier can be mixed with a suitable mixing device to form the 5th to 10th metal / support mixture. 5th to 10th! The metal / loaded mixture can be mixed using suitable mixing equipment. Suitable mixing equipment includes rollers, fixed shells or tanks, grinding mixers (such as batch or continuous), impact mixers, and can form the 10 Any other generally known mixer or generally known device for blocking metal / body mixtures

:: In a specific embodiment, the materials are mixed until the 5th to 10th columns of metal: shell are uniformly dispersed in the carrier. In some specific examples, after combining the support and the metal, the Tentacle is heat-treated at a temperature of 150 to 7500 t, 2000 to 7400 art, or 400 to 7 t. In some specific examples, the catalyst may be between 400 and 400 under the name of hot air and / or oxygen-enriched air. . And a temperature in the range of 1000 t to remove volatile substances, so as to convert at least a part of the first metal to the corresponding metal oxide. 72 200532010 ',,' and in other specific examples, the catalyst may be heat treated in the presence of air (for example, less than · t, less than ... Within a period of time, to remove most of the volatile substances without turning column…… gold: into metal oxides. # Catalysts prepared by this method are usually called catalysts.的 的 catalyst ° #Combined in this way to form a sulfide process: the catalyst 4 'active metal can be substantially dispersed in the carrier. For this type of catalyst: see the US patent case issued to Gabnelov et al. No. 2 1 8,333, and 6,29〇, 841 awarded to Gabriel ov et al. In specific examples t, the Θ oxide support can be combined with 帛 5 to ι ^ metal to form a Θ alumina support / No. 5 i 10 metal mixture. The alumina support / 5 to 10 metal mixture can be heat treated at a temperature of at least 400 ^ to form a catalyst with a pore size distribution with a median pore size of at least & 23 〇A. Typical In terms of this type of heat treatment, a temperature of up to 12,000 t is performed.

In some specific examples, the «body (commercial carrier or carrier prepared as described herein) may be combined with a supported catalyst and / or a bulk metal catalyst. In several specific examples, the 'supported catalyst may include a 15th metal. For example, the supported catalyst and / or bulk metal catalyst can be crushed into a powder having an average particle diameter of i to 50 microns' 2 to 45 or 5 to 4G microns. This powder can be combined with a carrier to form an embedded metal catalyst. In several specific examples, the powder can be combined with a carrier and then extruded using standard techniques to form a pore size with a median pore size in the range of 80 to 200 A or 90 to 80 A, or 20 to noa Distributed catalyst. 73 200532010 Contacting the catalyst with the carrier in a number of specific examples may &amp; &quot; separate metals exist beneath the surface of the buried metal catalyst + to V-in the part) 'and cause it to exist on the surface than by other methods. There is less metal in the carrier. In some specific examples, those who have less metal catalyst in the buried metal will extend the life and / or catalysis of the catalyst by allowing at least -2 surfaces to have a catalyst surface during use. Activity .: The metal is moved to the surface of the catalyst during the contact with the crude oil during the contact with the catalyst, and the catalyst surface can be removed by contacting and / or mixing the catalyst components at a number of specific estimates: surface. j Τ will make the 6th column = material ... the structure of the 6th metal in the cis structure of the random random order of the metal = catalyst can be determined using powder X-ray diffraction method. And metal oxidation: = The order of the :: order comparison of the order of the metal elements in the catalyst can be compared by comparing the order of the 6th metal peak in the X-ray diffraction spectrum of the object and the 6th block in the X-ray diffraction spectrum of the catalyst. The order of the metal peaks. From the disk X :, the line diffraction ㈣ With the widening and / or non-patterning of 6 metal-related patterns, it is possible to estimate the 6th metal that is substantially randomly arranged in the crystal structure. ^ For example, molybdenum trioxide and those with a median pore size of at least 1 80 people Alumina support can be combined to form an alumina / molybdenum trioxide mixture. Molybdenum trioxide has a clear pattern (such as clear Di00, D200, and ㈣d_wave-peak alumina / 6th dioxide mixture) Heat treatment at a temperature of at least 5 3 8 (丨 〇〇〇 卞) to produce a catalyst that does not show a molybdenum dioxide pattern in the X-ray diffraction spectrum (for example, without D 丨 ... wave peak). In specific examples, the catalyst may be characterized by a pore structure. Various parameters of the pore structure include, but are not limited to, pore size, pore volume, and surface area. 74 200532010 or a group of sigma catalysts may have a total pore size distribution relative to the pore size. Pore size The median pore size of the distribution can be in the range of 30 to 1,000 people, 50 to 500 people, or 60 to 300 A. In several specific examples, each gram of catalyst contains at least 0.5 grams of gamma alumina The catalyst has a median pore size of 60 to 2 A; pore size distribution in the range of 90 to 180 A, 100 to 140 A, or 120 to 13 A. In other specific examples, a catalyst containing at least 01 g of gadolinium alumina per gram of catalyst has a median pore size At 180 to 500 A, 200 to 300 A,

Or within the range of 230 to 250 A, your eight A heart sacrifice the pore size distribution. In several specific examples,

The median pore size of the pore size distribution is at least 19 Λ XJ Ding 1 Zashi Wang / Ma 12〇A, at least 150 people, at least ⑽, at least 200 Α, at least 22 〇A, at least 23 〇 , Or at least 300A. This type of median pinch is typically at most negotiated. The catalyst may have a pore size distribution with a median pore size of at least A λ Xi Ma 60 A or at least 90 A. In some specific examples, the touch-out nozzle media has a median aperture of 90 to 1 80

A, the pore size distribution within 100 to 140 people, or 120 to X-i 30 people, at least 60% of the total pore plate in the pore size distribution

The 数 number has a pore size in the range of 45 A, 35 A, or 25 A median pore size. In the specific examples of #, the catalyst has a pore size distribution with a median pore size ranging from 70 to 180 A. At least 60% of the total number of pores in the pore size distribution has a lambda x x 45. Aperture in the median aperture range of human, 35 A, or 25 A. In the pore size distribution, the median pore size is at least 180 A, at least 200 people, or at least 230 people. In the specific example ^, in which more than 60% of the pore size distribution has a total number of 50 A, 70 A, pore size within the median pore size range of Formula One or 90A. In some specific examples, the angular catalyst has a median pore size in the range of 180 to 500 A, 200 to 400 A, or 230. 1 5 230 to 300 people with a pore size of 75 200532010. The pore size distribution is at least 6 0% of the total number of pores has a pore size that is also in the range of A, Chuan, or 90 A. In several specific examples, the pore volume of the pore may be at least, 3 at least 0.7 cm3 / g, or at least cubic. 0 3 / .., m / g g and 0.9 cm / g. In a specific embodiment, the pore volume of the pores can be in the range of 0.3 to 0.99 cmVg, 0.4 to 0.7 cm to 0.7 cm3 / g. G, 0.5

Catalysts having a pore size distribution with a median pore size in the range of 90 to 18 OA may have at least 100 m2 / g, at least m / g, at least 170 m2 / g, and at least 22 in some specific examples. The surface area of m2 is determined to be 270 m2 / j. Such surface areas can range from 100 to 300 m to 27 (m / g, 130 to 250 m2 / g, or 170 to attentive pressure). In specific embodiments, median pore sizes range from 180 to 300A. The catalyst with a pore size distribution within the range may have a surface area of at least 60 m2: ≧ 100 m2 / g, at least 120 m2 / g, or at least a surface area of this type. Such surface area may be at 60 To 30〇1112 仏, 90 to 100 to 270 mVg, or 120 to 250 m2 / g. G

. In a specific embodiment, the catalyst exists in a shaped form, such as a pellet shape, a cylindrical shape, and / or an extrudate. The catalyst typically has a range of up to 500 N / cm, 60 to 400 N / cm '100 to 350 N / cm, 200 to 300 N / cm, or 220 to 280 N / cm. Shatter strength of the inner plate. In some specific examples, catalysts and / or catalyst precursors use technologies known in the technology (such as ACTICATm method, CRI International,

Inc.) is vulcanized to form metal sulfides (before use). In several specific examples, the catalyst can be dried and then vulcanized. Alternatively, the catalyst can be vulcanized on-site by contacting the catalyst 76 200532010 with a crude oil feed containing sulfur-containing compounds. Vulcanization can be performed in the presence of hydrogen with a cadaver, or a liquid-phase vulcanizing agent, an organic sulfur compound (including surface sulfur, ... ^ For example, the off-site vulcanization method is described in ^ Yafeng) 5 468 377, The U.S. Patent No. of Mans Temples, issued to Sea, ns and others 5,688,736. With ::: In the specific example, the first-type catalyst ("the first-type catalyst,") contains the 5th to 10th metal of the ΐ 25ΓΓ mouth, and has an order aperture within the range of 150 to 250 A. Kong Yan talked about scholars, Dao Shendi a catalyst can have at least 100

„Insertion area: The pore volume of a catalyst can be at least 0.5 cm3 / g. = Heavy shots have a gamma oxide content of at least 5 g of gamma alumina per gram of first catalyst, A maximum of 0.099 grams of rhenium alumina. There are several catalysts in Ang 雕 奋, "In the case, there are 0.0001 to

ο · 1 gram range of the 6th person H ^ ,, .. α1 total content of Mon. The first catalyst can remove ^ Γ — ^ Ni / v / Fe, remove the rule that caused the crude oil feed Γ ;: component 'removed at least-part of the crude oil in the crude oil feed ... Medium to small one 5 or 1 4 A less than one metal in the form of a metal salt of an organic acid,

〆 ”and 〇 When the crude oil such as Hachiman / Yi was exposed to a catalyst, other properties (eg, Stone claw $, VGO content, may show only a relatively small amount of double, residue content 'or a combination thereof). Sex # &amp; Li, Aihua. Can selectively change the crude oil feed J 丨 Wang Bei while at the same time · mouth 0 Α, to perform more effectively: change other properties can allow crude oil feed catalyst can be arbitrary: sequence Use :: in the specific example '-or multiple first-species in a specific specific example, Chu — ί and the carrier's enthusiast, the first catalyst (“the second catalyst,”) contains and, The 5th to 15th a η ⑶ metal of the mouth has a pore size distribution with a median pore diameter within the range of h from 90 to 180 77 200532010 A. The total number of pores and the distribution of pores are at least such that they have a median pore size range of 45 A. Under contact conditions, the original, ▲ W ″, t are the holes of Figure M. Under the appropriate conditions, the crude oil feed has the same properties as the contact feed of the second catalyst, and-the production and crude oil, ^ the selection is subject to change, and at the same time other properties &amp; raw shellfish ( For example, TAN) / IA ^ 改变 changes in crude oil products. In the case of Yu Qianqian, the source of hydrogen may be present during the contact. Dry, ... The first kind of catalyst can reduce the M component that causes the crude oil feed ′ which results in a relatively high viscosity of at least-part of the knife, at least a part of the N / X crude oil production 3 miles. In addition, the contact of the crude oil feed-heavy: medium contact can produce crude oil products with varying amounts of sulfur compared to the sulfur content of the crude oil feed. For example, crude oil products; compared with sulfur-containing crude oil feeds containing 70% to 130% of crude oil feeds in Guari, the distillate content, ν :: a product and 3 miles VCj〇 combined, and residual In terms of material content, it may show only a small change. In several specific examples, the crude oil feed may have a relatively low I / F: (e.g., up to 50 wtppm), but a relatively high TAN, asphaltene content, or metal content in the form of a metal salt of an organic acid. Relatively high M, (e.g., at least 0.3 A) may make crude oil feed unacceptable for transportation and / or refining. Has relatively high. Inferior crude oils with 5 cyanin content may show lower stability during processing compared with other crude oils with relatively low 溽 音 皙 晷 &amp;# π, Zhong Huan must% & Yuebei 3 . The contact of the crude feed with the second catalyst can remove the acidic components of the crude feed that cause TAN and / or C5 asphaltenes. In some specific examples, 'reducing c5 asphaltenes and / or the constituents that cause TAN compared to the viscosity of the crude oil feed may reduce the viscosity of the crude feed / total product mixture by 78 200532010. In specific examples, it is used to deal with the stability of one or more combinations of +, AA, and various catalysts described in this article. draw. W plus catalyst life, π right-hander who provides hydrogen for crude oil feed. · In J, Aλ. "" By the carrier and the metal in column 6 :: catalyst: third catalyst " ) Can be obtained by the precursors can be obtained at one or the night ° catalyst precursors. Catalyst (for example, less than 482. 0 = less than 500 t of uncalcined in the presence of a compound: ... heat: a relatively short period of time to produce at least 100 ° C, prime 9 D, The catalyst flooding system is heated to ^ k °. In the specific embodiment, the second type is pulled out, and the mother gram catalyst can have 0 001 stone. One type of catalyst is 〇008 · to 0.03 g, 0.005 to 0.02. Gram, or the second within the range of • 01 grams, when used to deal with what has been done in this article ... Blocker containing Xia. The three catalysts μ. R ^ .. can show significant activity and sharpness when feeding crude oil. %. In some cases, the catalyst precursor is heated in the presence of one or more sulfur compounds on the night of the night-at temperatures below 500 t. The three catalysts can be Reduce at least the components of the UN that cause crude oil feed, reduce the metal in the form of organic acid metal salt of at least -eight ^ i knife s ^ ^ D knife, reduce: Fe content of oil products, and reduce the viscosity of crude oil products. In addition, The contact of taxis, oil feeds and a third catalyst can produce a sulfur ratio with crude oil feeds': its sulfur content A relatively small change in crude oil product with relative absorption of hydrogen with crude oil feed. For example, a crude oil product may have a sulfur content of 70% to 130% of the crude oil feed. Use a third catalyst Compared with the crude oil produced by Panmei A, and crude oil, the crude oil product may also show only changes in the proportion of API, fraction VGO 3, and residue content that are comparable to 79 200532010 2. Reduce crude oil input The ability to feed &amp; TAN, organic acid metal salt in the form of Ni / V / Fe s, and the viscosity while only slightly changing the A &quot; specific gravity, ::: ⑽⑽, and residue content can allow crude oil products to be various Used by processing equipment. One or three catalysts can reduce the red R content of crude oil feed by at least: part t in several specific examples, while maintaining the stability of the crude oil feed / total product. In a specific specific example, the third The catalyst can present the metal content of the 6th block in the range of-^ to g, please 5 to ⑽, or ⑽ 丨 to please 1 and the amount of G to Q G5 gram per gram of catalyst. 〇〇5 to 0. 03 grams, or 〇〇〇〗 to 0 01 grams Jindan ^ See the dry fence Brother 1 〇 metal ri. Brother Y and 10 columns of metal catalyst can promote reducing at least a part of the temperature in the range of 300 ^ 500 1 or 350 to 450 t and 0.1 to 10 2 feed 1 to φ 8 MPa 'or the pressure in the range of 2 to 5 Mpa caused the composition of the original / from the MCR in the feed. In: specific examples, the fourth type of catalyst ("fourth catalyst, including Kong Ping, The fifth metal block combined with the Lv carrier. The fourth type: = pore size distribution. In some specific examples, the fourth median pore length can be at least 22. The carrier may be at least-, at least 〇1, or at least _A °. The carrier may contain at least 0.5 g, at least ancient &quot; per gram of carrier. The fourth catalyst may or may be Ding Jie in some specific examples. The example may contain up to 5.5% of the metal in each gram of catalyst, and at least 0.0001 grams per gram of catalyst. Of the genus. In a specific embodiment, the fifth metal is thallium. ; The right dry concrete shot ’After contact with the fourth catalyst, the crude oil 80 200532010 feed can be contacted with the additional catalyst. The first catalyst, the second catalyst, the fifth catalyst, the sixth catalyst, the product catalyst, or a combination thereof. The additional catalyst may be one or more of the following catalysts, a third catalyst, a fourth catalyst, a seventh catalyst, and a number of specific examples described in this article. J r wind can be used in crude oil feed and The fourth catalyst contact period is from 300 to 400. Wide, q A 1 4⑽C, 32 ° to 38 ° t, or 33 ° to 370 ° C. From this type

The crude oil products produced by such contact may have 90% of D1S, most of which are only 0 / Tian Yu Xifeng 80 /. , The maximum is 50%, or up to 10%

The TAN of the crude feed. Hydrogen generation can occur at 45 ° Nm3 / m3, i0L4.

Nm / m3 'or 15 to 25 Nm3 / m3. Crude products may have a total Ni / V / Fe content of up to 900 / day. ^ Take Xima 90 / 〇 take 80. / 〇, up to ‘is 70〇 / 〇, Yuan Xi is 50%’ up to rabbit in〇 /-vs »from 10 / 〇, or at least 1% of crude oil

Ni / V / Fe content.

In a specific specific example, the fifth type of catalyst ("the fifth catalyst, ... the sixth metal that is combined with theta oxide body. The fifth catalyst has a meso 4 pore size of at least 180 A and at least 220 A, at least 23〇a, at least "250 A 'at least 300 A' or at most 500 A, the pore size distribution body may contain at least 0.1 g, at least 0.5 g per gram of carrier, Or 0.999—gram of θ oxidation in Lu. In some specific examples +, the carrier has an alumina content of less than 0 ″ g per gram of catalyst. Α catalyst is included in the specific examples. In the catalyst, there is a maximum of 1 gram of the /, and /, and the mother gram catalyst has at least 0 0001 grams of the sixth metal K. In the specific example, the metal in column 6 is molybdenum and / or tungsten. In the example, when the crude oil feed is in contact with the fifth catalyst at a temperature of 3 81 200532010 to 400 t :, 320 to 370 t ;, or 33 to 36, the net absorption of hydrogen from the crude feed may be Quite low (e.g. 0.01 to 100 Nm3 / m3, 1 to 80 Nm3 / m3, 5 to 50 Nm3 / m3, or 10 to 30.

Nm3 / m3). The net uptake of hydrogen from crude oil feeds can range from 20 Nm / m, 2 to 15 Nm3 / m3, or 3 to 10 Nm3 / ni3 in several specific examples.

Inside. The crude oil product produced by contacting the crude oil feed with the fifth catalyst may have a TAN of up to 90%, a maximum of 80%, a maximum of 50%, or a maximum TAN of the crude feed. The TAN of the crude product may be in the range of 0.01 to 0.03 to 0.05, or 0.02 to 0.03.

In a specific specific example, the sixth type of catalyst ("the sixth catalyst,") includes the fifth column metal and the sixth shelf metal combined with a Θ alumina carrier. The sixth ceremony catalyst has a median pore size of at least $ 18〇A pore size distribution. In several examples, the median pore size of the pore size distribution can be at least 22 OA, at least A, at least 250 A, at least 300 A, or up to 500 A. The carrier may contain at least 0 "grams, at least 0.5 grams, at least 0" grams, at least 0.9 grams, or at most 0.99 grams of theta oxide per gram of carrier. In some specific examples, the carrier may include the total amount of the first metal and the sixth metal of column Q i 1 per gram of the catalyst, and at least the fifth metal and the sixth metal per gram of the catalyst. The total amount of metal. In some specific examples, the molar ratio of the total amount of the 6th metal to the total amount of the 5th metal may be in the range of ο ″ to μ, 1 to ′, or 2 to 5. In a specific embodiment, the first metal is rhenium and the sixth metal is molybdenum and / or tungsten. . When crude oil is fed with the sixth catalyst at 310 to 400. 0, 32 to 37 ° C, or 330 to 360. When contacted at ⑽ temperature, the gas of crude oil feed 82 200532010 can be absorbed from -10 Nm3 / m3 to 20 Nm3 / m3, 7 Nm3 / m3 to

Nm3 / m3 'or · 5 Nm3 / m3 to 5 NmVm3. Negative net uptake of nitrogen is an indication that hydrogen is being produced on site. The crude oil product produced by contacting the crude oil feed with the sixth catalyst may have a TAN of at most 90%, at most, at most 50%, at most 10%, or at least 1% of crude oil feed. The TAN of the crude product may be in the range of 0.001 to ο ", 0.02 to 0.05, and 0.04.的 A small net uptake of hydrogen during contact of the crude feed with the fourth, fifth, or sixth catalyst will reduce the overall demand for hydrogen during processing to produce and / or process acceptable crude oil products. Since the cost of producing and / or transporting hydrogen is expensive, minimizing the amount of hydrogen used in the process will reduce the overall processing cost. In a specific specific example, the seventh type of catalyst (the "seventh catalyst") has a total metal content in the sixth column of the sixth metal barrier ranging from 0.001 to 0.66 grams per gram of catalyst. Inside. The sixth metal is molybdenum and / or tungsten. The seventh catalyst system is conducive to the production of crude oil products of TAN with a crude oil feed of TAN of up to 90%. Other specific examples of the first, second, third, fourth, fifth, sixth, and seventh catalysts can also be manufactured and / or used as described elsewhere herein. The remote selection of the catalysts and control of operating conditions of this application may allow the production of crude oil products with altered TAN and / or selected properties compared to the crude oil feed while other properties of the crude oil feed do not change significantly. The resulting crude oil product may have enhanced properties compared to the crude oil feed and is therefore more transportable and / or refined. Configuring two or more catalysts in a selected order can control the order of improving the properties of the crude oil feed. For example, TAN, specific gravity, at least a portion of q asphaltenes, at least a portion of iron, ^ #,, ,, and / or at least a portion of vanadium in a crude oil feed can reduce at least one of the crude oil feed. The heteroatoms in Part 8 were reduced before. Knife configuration and / or selection of catalyst in several specific examples can improve catalyst life and / or stability of crude oil feed / total product mixture. Improve during processing

The life of the catalyst and / or the stability of the crude feed / total product mixture may allow: The catalyst system to operate for at least 3 months, at least 6 months, or at least 1 year without changing the catalyst in the contact zone. Before the other properties of the crude oil feed are changed, the coupling catalyst can make at least a part of Ni / v / Fe in the feed, at least a part of ^^^, and at least a part of the organic acid metal salt form. Metals, at least a portion of the ingredients that cause TA + N, at least a portion of the residue, or a combination thereof are reduced, as well as maintaining a stable crude oil feed / total product mixture during processing

(J, keep the marginal, p-value of crude oil feed of 1.5). Alternatively, the specific gravity of C5 asphaltenes, TAH and / or AP may be rt »7K, which is gradually reduced by the contact between the crude oil feed and the selected catalyst. The ability to change the properties of the crude feed incrementally and / or selectively 14 may allow the stability of the crude feed / total product mixture to be maintained during processing. In the case of dried octopuses, the first catalyst (the above) can be arranged upstream of a series of catalysts. This configuration of the catalyst can allow the removal of high-molecular pollutants, metal fouling, metals in the form of R-wood, and / or organic acid metal salts, while maintaining crude oil feed Inch ten / ~ Product mixture stability. 84 200532010 The first catalyst, in several specific examples, allows the removal of at least a part of the ISH / V / Fe in the crude oil feed, the removal of acidic components, the removal of components that shorten the life of other catalysts in the system, or combination. For example, compared to crude feed, reducing at least a portion of the asphaltenes in the crude feed / total product mixture will inhibit the clogging of other catalysts placed downstream, thus increasing the number of contact systems in the absence of supplemental catalyst Down for the duration of operation. Removal of at least a portion of the Ni / V / Fe in the crude oil feed in several specific examples can increase the life of one or more catalysts placed behind the first catalyst. The second catalyst and / or the third catalyst may be arranged downstream of the first catalyst. Further contact of the crude oil feed / total product mixture with the second catalyst and / or the third catalyst can further reduce the TAN, reduce the Ni / v / Fe content, fight for low S, and reduce oxygen content! And / or reduce the metal content in the form of metal salts of organic acids. In some specific examples, the contact of the crude oil feed with the second catalyst and / or the third catalyst can produce a crude oil feed / total product mixture. Compared with the individual properties of the crude oil feed, it has Reduced TAN, reduced sulfur content, reduced oxygen content, reduced metal content in the form of metal salts of organic acids, reduced asphaltene content, reduced viscosity 'or a combination thereof, while maintaining crude oil feed during processing / Total product mixture stability. The second catalyst can be arranged in parallel. The second catalyst is located upstream of the third catalyst, or vice versa. The ability to transport hydrogen to the 4th corner of Jiaoshu District will tend to minimize the amount of chlorine used during contact. Combined with the catalyst that promotes the occurrence of hydrogen during the contact Wu's catalyst that absorbed a relatively small amount of hydrogen during the contact can be used to change the initial properties of crude oil compared to the same properties of the crude oil 85 200532010 feed. For example: The catalyst can be combined with the first catalyst, the second catalyst, the first catalyst, the fifth catalyst, the sixth catalyst, and / or the seventh catalyst == to change Selected properties of the crude oil feed, while at the same time only changing the other properties of the original: feed in a selected amount, and / or maintaining the conversion of the crude oil feed / total product at the same time. The order and / or number of catalysts can be selected to minimize the net uptake of hydrogen: the stability of the crude oil feed / total product. The minimum net absorption of hydrogen is the residue content, VG0 content, fraction content,

The specific gravity 'or a combination thereof is kept within the range of individual properties of the crude oil feed, and the TAN and / or viscosity of the crude oil product is at most 90% of the TAN and / or viscosity of the crude oil feed. Reducing the net uptake of hydrogen by crude oil feed can produce crude oil products that have a process similar to the distribution of the fodder point of the crude oil feed, compared with the tan of the crude oil feed> tan. The atomic H / c of crude oil products can also be changed only slightly compared to the atomic H / C of crude oil.

The generation of hydrogen in a particular contact zone may allow selective addition of chlorine to other contact zones and / or allow selective reduction of the properties of the crude feed. In several specific examples, the fourth catalyst may be disposed upstream, downstream, or between the additional catalysts described herein. Hydrogen can be brought into contact with the fourth catalyst in the crude feed-within a month, hydrogen can be transported to the contact zone containing additional catalyst. The transport of hydrogen can be reversed from the flow of the crude feed. In several specific examples, the rotation of hydrogen may be in the same direction as the flow of crude oil feed. For example, in a stacked structure (see Figure 2B), hydrogen may be generated during a contact in a contact zone (such as contact zone 102 in Figure 2B), and hydrogen may be transported in the opposite direction of the crude oil feed flow 86 200532010 To additional contact areas (such as contact area 114 in Figure 2β). In several specific examples, the hydrogen flow may be in the same direction as the flow of the crude oil feed. Alternatively, in a stacked structure (see Fig. 3B), hydrogen may be generated in a contact region (such as the contact region 102 in Fig. 3B) during the contact. The hydrogen source can be transported to the first additional contact zone in the opposite direction of the crude oil feed flow (for example, in FIG. 3B, hydrogen is added to the contact zone Π4 via the conduit 106). Two additional contact areas (for example, in FIG. 3B, hydrogen is added to the contact area ιι6 via the conductive f 061). In several specific examples, the fourth catalyst is used in parallel with the sixth catalyst system, and the fourth catalyst system is located upstream of the sixth catalyst 'or vice versa. The combination of the fourth catalyst and the additional catalyst can reduce the TAN, reduce the job content, and / or reduce the metal content in the form of a metal salt of an organic acid in the case of a small net absorption of hydrogen from the crude oil feed. The small net uptake of gas allows for minor changes in other properties of the crude product. The same properties of I crude oil are compared in only a few specific examples, two of which are used. The force μ »π U of the seven catalysts can be combined so that the seventh catalyst used upstream instead of the lower catalyst can have 0 to G G6 gram catalyst in the total mother content. The sixth metal in the seventh kind of catalyst in the downstream and the metal A in the seventh kind of catalyst in the mother gram can be at least larger than the seventh kind of catalyst in the upstream or the mother gram catalyst in the seventh. .〇2 支] Metal t 3 miles. In some concrete examples of the sixth metal block that contains + metal, the upstream catalyst can be reversed. The ability of the next catalyst and the seventh seventh catalytically active metal can be as follows: other properties of the catalyst using a relatively small amount of μ 'products are compared to the same properties of the crude oil 87 200532010 feed σ API t 卜 f (for example Heteroatom content, APί specific gravity, residue content, and VG0 content were changed in 3). Or a relatively small amount of crude oil feed with upstream and downstream has a maximum of TAN? The contact of the seven different catalysts can be produced or at least]. It is 80%, up to 50%, and up to ㈣. In the example of TAN, 弇 仏, and 弇 仏, which are 1/0 of the crude oil feed, the crude oil feed is divided into several specific M ^ 4. -^ Τ 糟 is gradually reduced by the contact of /, the upstream and downstream seventh catalyst (for example, Panyuyuan, the contact between Jinke and the catalyst to produce the product magic / virgin crude oil products with altered properties' then The contact system of i ΓΓ media produced by the crude oil has a change compared with the crude oil product: = product). The ability to progressively reduce the TAN maintains the stability of the crude feed / total product mixture during processing. The combination of 'catalyst selection and / or catalyst sequence and control of contact conditions (such as temperature and / or primary flow rate by flow rate) in dried octopus cases can help reduce the amount of chlorine It absorbs 'helps to maintain the crude oil feed / total products during processing' and changes compared to the individual properties of the crude oil feed. The stability of the crude feed / total product mixture w Z% θ in turn affects the various phase separations from the crude feed / total product mixture. Phase separation may be caused by, for example, the insolubility of crude oil feed or crude product in the crude oil feed / total product mixture, the transfer of crude oil feed / total product mixture, precipitation of ingredients in the reduced crude oil feed / total product mixture, or a combination thereof resulting in. The concentration of crude oil feed and / or total product in the crude oil feed / total product mixture may vary during a certain number of contact periods. When the total product concentration in the crude oil feed / total 88 200532010 product mixture changes due to the formation of crude oil products, the solubility of the crude oil feed ingredients and / or total product ingredients in the crude oil feed / total product mixture will tend to change. For example, a crude oil feed may contain: components that are soluble in the crude oil feed at the beginning of processing. When the quality of the crude oil feed (such as TAN, MCR, C5 asphaltenes, p-values, or a combination thereof) changes, these ingredients may tend to become less soluble in the crude oil feed / total product mixture. In several examples, the crude feed and total product may form two phases and / or become insoluble with each other. Changes in solubility may also cause the crude feed / total product mixture to form two or more phases. Due to the flocculation of asphaltenes, changes in the crude oil feed and total product concentration, and / or sedimentation of the constituents, two phases tend to reduce the life of one or more catalysts. In addition, process efficiency can also decrease. For example, the raw material mixture may be repeatedly processed to produce a crude product with desired properties. + ~ Product ▲ During processing, the p value of crude oil feed / total product mixture, process, crude oil feed, and / or crude oil feed / total product mixture = 'can be monitored. Typically, the maximum MMP value indicates that the flocculation of the crude oil feed usually occurs. If the P value is at least 15 at first, the value will increase or be fairly stable during the contact period, then this means that the original / ', during the contact period ... Stability of crude oil feed / total product mixtures, such as %%, can be controlled by controlling the contact conditions, by the catalyst = 'selective ordering of the catalyst, or a combination of Be controlled. ^ The contact conditions of the industrial system may include controlling the LHSV, temperature, pressure, and hydration. Absorption :: oil feed flow rate, or a combination thereof. 2. In the specific example of the right stem, control the contact temperature in order to remove c5 cyanide 89 200532010 and / or other asphaltenes, and keep the MCR content of the crude oil feed. If two phases are formed, it can reduce the MCR content by lowering the contact temperature, which may be conductive and / or-or multiple catalysts; Shou 1 Yuan ;: mixed feed / total product 产物 ^ ^ ^ x ^ ^ p The combination of temperature and hydrogen uptake-the catalysts charged herein may allow for a small change in the MCR content of the crude oil feed. n In several specific examples, the temperature in the contact zone can be used to make contact conditions in order to make one or more contacts ^, ,,,, 4 ,, etc. Operation at different temperatures may allow selective changes in the feedability of the crude oil for a period of time η, Λ—belt to maintain the stability of the crude oil feed / total product mixture. The crude feed enters the first contact zone at the beginning of μ. The first contact temperature is the temperature in the first contact zone. Other contact temperatures (e.g., second temperature, third temperature, fourth temperature, etc.) are the temperatures in the contact area disposed behind the first contact area. The first contact temperature may be in a range of 100 to 420,000 t, and the second contact temperature may be 20 to 100 different from the first contact temperature. . , In the range of 30 to 90 C or 40 to 60 t. In some specific examples, the second contact temperature is greater than the first contact temperature. Having different contact temperatures can reduce the @TAN and / or c5 cyanide content in the crude product to a ratio compared to the TAN and / or A asphaltene content of the crude feed, if any, in the first and The TAN and / or C5 asphaltenes are reduced to a greater extent when the second contact temperatures are the same or differ by less than 10 ° C. For example, the first contact area may include a first catalyst and / or a fourth catalyst &apos; and the second contact area may include other catalysts described herein. The first contact temperature can be 350 ° C, and the second contact temperature can be 300 t. Contact of the crude oil feed with the first catalyst in the first contact zone and / or contact with the fourth catalyst at a higher temperature before contact with other catalysts in the second contact zone 200532010 may result in In the crude feed, there are more TAN and / or 匚 5 asphaltenes compared to the decrease in TAN and / or q asphaltenes in the same crude oil feed when the first and second contact temperatures differ by less than 10 ° C. Reduction. Examples The following are non-limiting examples of carrier preparation, catalyst preparation, and a system having a selected catalyst configuration and controlled contact conditions. fExample 1 · Prepare for contact and contact. The carrier system uses 585 grams of water and 8 grams of glacial nitric acid to reduce 576 grams of aluminum oxide (Criterion Catalysts and Technogies Lp).

City, Michigan, U.S.A.) was prepared by milling for 35 minutes. The resulting milled mixture was extruded through a 1.3 TrilobeTM template, dried between 90 and 25, and then calcined at 918 ° C to obtain 650 g of a calcined support with a median pore size of I82 people. This calcined support was placed in a Lindberg furnace. The temperature of the furnace was raised to 1,000 to 11,000 during 1.5 hours, and then kept in this range for 2 hours to produce a carrier. This carrier contains 0-0003 grams of gamma alumina, 0.008 grams of alumina, 0.0008 grams of s_alumina, and 0.978 grams of theta alumina per gram of carrier. Determined by \ ray diffraction. This support has a surface area of 110 m2 / g and a total pore volume of 0.82 cmVg. This carrier had a pore size distribution with a median pore size of 232 A, and 66.7% of the total number of pores in the pore size distribution had a pore size in the range of 85 people. This example illustrates how to prepare a support having a pore size distribution of at least 180 A and containing at least 0.1 g of Θ alumina. For example, the diameter of the wide seat should be at least ― pore size 91 200532010 1. The rhenium catalyst was prepared in the following manner. By example! The prepared oxide carrier was impregnated with a rhenium immersion solution, which was prepared by combining 7,69 g of vosw and 82 g of deionized water. The value of this solution was 2 27. Oxide Shao carrier (100 g) was impregnated with osmium immersion solution to accidentally induce aging for 2 hours. Dry at 25 ° c for several hours, and then thoroughly. . Simmer for 2 hours. The obtained catalyst contained 0 g of vanadium per gram of catalyst, and a part was used as a carrier. This rhenium catalyst has a surface area with a pore pinch distribution of a median pore size of $ A and a pore volume of 0.69 cm3 / g '* nom2 / g. In addition, in the pore size distribution of the sharp catalyst, 66 7% of the total number of pores had a pore size within the range of the meso pore pinch. This example illustrates the preparation of a column 5 catalyst having a pore size distribution with a median pore size of at least 4 230 A. Kongm ^ iilii catalyst with a diameter of at least j3〇 A. The indium catalyst is prepared in the following manner. The emulsified carrier prepared by the method described in Example 1 was impregnated with a rhenium immersion solution. This infusion solution was combined with 4.26 grams of (ΝΗ4) 2MO207, 6.38 grams of MO3, 112 grams of 30% H202, and 0.27 grams of monoethanolamine (MEA). , 6.51 grams of deionized water was prepared to form a 'moxibustion solution. This slurry was heated to 65. . Until the solids are dissolved. The heating solution was allowed to cool to room temperature. The pH of the solvent was 5 36. Adjust the solution volume to 82 mL with ionized water. The alumina carrier (100 g) was impregnated with a molybdenum impregnating solution, aged by accidental agitation for 2 hours, dried at 125 hours for several hours, and then taken at 2 480 t 92 200532010. The catalyst contained in the catalyst contains 0. g of platinum per gram of catalyst, and the remainder is a carrier. This molybdenum catalyst has a pore volume of a median pore diameter of 25 Å, a pore volume of 0.77 cm / g, and a surface area of j J 6 m2 / g. In addition, the pore size distribution of the molybdenum catalyst had a total number of pores of 67.7% having a pore size in the median pore size range of 86 persons. This example illustrates the preparation of a sixth catalyst having a pore size distribution with a median pore size of at least 23 A. Nine ^ Example 7-System A has a median hole. You must have a hole diameter of at least 230 A. Search for earth molybdenum / button contact. The molybdenum / vanadium catalyst was prepared in the following manner. The alumina support prepared by the method described in Example 丨 was impregnated with a molybdenum / vanadium impregnation solution prepared as follows. The first one is that by combining 2.14 g of (NH4) 2M0207, 3 21 g of M03, 0.56 g of 30% hydrogen peroxide (n), and 14 g of single Ethanolamine (MEA) is manufactured by forming a slurry with 3.28 grams of deionized water. This slurry was heated to 65 C until the solids were dissolved. The heating solution was allowed to cool to room temperature. The second solution was made by combining 3.57 grams of deionized water from 0804 and 40 grams. The first solution was combined with the second solution [adding sufficient = deionized water to bring the volume of the binding solution to 82 ml to produce a molybdenum / vanadium immersion solution. The oxide was impregnated with a flip / plump immersion solution, aged by accident for 2 hours, dried at 125 t for several hours, and then calcined at 48 0 t for 2 hours. The obtained catalyst contained # 〇〇2 {of vanadium # 口 〇〇2 g per gram of catalyst

Molybdenum, the rest is the carrier. This molybdenum / vanadium catalyst has a pore size distribution with a median pore size of 3㈧A. This example illustrates the preparation of a 6th metal and a 5th metal catalyst having a pore size with a median pore size of at least 230 A. Example 5 · ~~ MJtJM is equipped with a three-box reactor. A tubular reactor equipped with a temperature measuring sleeve at the center is equipped with a thermocouple to measure the temperature of the entire catalyst bed. The catalyst bed is formed by filling the space between the temperature measuring sleeve and the inner wall with catalyst and silicon carbide (20_grid, stanford Matenals; AllS0 Vlej0, CA). It is believed that this silicon carbide, if any, has low catalytic properties under the operating conditions described herein. Prior to placing the mixture in the contact zone of the reactor, all catalysts were blended with an equal volume of silicon carbide.

The reaction crude oil feed flow system is from the top of the reactor to the reactor white bottom flint reversed silica system is arranged at the bottom of the reactor as a bottom carrier. The catalyst / silicon carbide mixture (42 cm3) at the end of the year is placed above the silicon carbide to form a bottom contact area. The bottom catalyst has a pore size distribution with a median pore size of 77 A, and 66 7% of the total number of pores in the 50 pore size distribution has a pore size within the range of A's median pore #. The bottom catalyst contained 0.095 g of molybdenum and 0.025 g of # 'per gram of catalyst, and the remainder was an alumina carrier.

The middle catalyst / carbon cut mixture (56 em3) is placed above the bottom contact area to form the middle contact area. The intermediate catalyst has a pore size distribution with a median pore size of 98 Λ. In this pore size distribution, "6.7% of the total number of pores has a pore size within the range of 24 Α median pore diameter. Contains 0.02 gm and 0.08 gm, and the rest is an oxide carrier. &Amp; Page. The catalyst / silicon compound (42 cm3) of P is arranged above the middle contact area to form the top contact area. The top catalyst has a median pore size of 192A scoop hole k-knife cloth '. Each gram of the catalyst contains 4 g of molybdenum, and the rest is mainly 94 200532010. It is a gamma alumina carrier. The top of the zone is filled with vacancies and serves as a preheating zone. The catalyst bed is loaded into the Lindberg furnace, which includes five heating zones corresponding to the preheating zone, top &quot; 卩, middle 'and bottom contact zones, and the bottom carrier. The medium is introduced by introducing a gaseous mixture of 5 vol% hydrogen sulfide and 95 vol% hydrogen at a rate of 1.5 liters of the gaseous mixture per unit volume (mL) of the catalyst (silicon carbide is not considered as a volume part of the catalyst). Contact zone to form a sulfide contact zone at a temperature of 1 During the process, the temperature was increased to 204 ° C (400.1?) And kept at 204 ° C for 2 hours. After holding at 204 ° C, the contact zone gradually increased at a rate of 10 ° C (50 ° F) per hour. To 316 t (600 F). Keep the contact area at 316. In the next hour, they gradually rose to 370 in the next hour (700) and kept at 2700% to make the contact area. Cool to ambient temperature. Filter crude oil from the Mars rig in GulfOfMexico, then heat it in a supply tank for 12 to 24 hours at% t (fan. F) to generate a crude oil with the properties shown in Table 17 in summary. Feed the crude oil feed to the top of the reactor. The crude oil feed flows through the preheating zone, the top contact zone, the middle contact zone, the bottom contact zone, and the bottom carrier of the reactor. The crude oil feed is stored in the chlorine gas reservoir and Each catalyst is contacted. The contact conditions are as follows: the ratio of hydrogen to the crude oil feed to the reaction is 328 Nm3 / m3 (200 SUB), the recommended V is 1 h-, and the pressure is 69 MPa. It is a stone. W. U A contact area is added ... to 3 70 C (700. |?) And is accompanied by a 3 7 Λ. Guangy ^ and the symbol is 500 hours at 370 C. The temperature in each contact zone was then increased and maintained in the order of j shells (· 379 ° CF) for 500 hours, followed by 388. u (/ 30 F) for 500 hours, 95 200532010 followed by 390 t (734 T) for 180 hours , Followed by the outer T) 2400 hours. (? 42 total products (in other words, crude oil products and gases) leave the catalyst bed. The total products are led to a gas phase liquid separator. In a gas-liquid separator, the total product is separated into a crude product and a gas. The system's gas input is measured by a mass flow cardiac device. The gas system leaving the system is determined by a hygrometer. Crude oil products are regularly analyzed to determine the weight percentage of crude oil product components. Results listed are averages of measured weight percentages. Crude product properties are summarized in Table 1 of FIG. As shown in Table 1, the crude oil product has a sulfur content of 0.0075 grams per gram of crude oil product, a residue content of 0.255 grams, and an oxygen content of 0.0007 grams. The crude oil product has TANs with a ratio of MCR content to C5 asphaltene content of h9 and 0.09. The total amount of recorded and vanadium is 22.4 ^ Chong. The catalyst life is determined by measuring the weighted average bed temperature ("WABT") against the original and the feed operating time. The catalyst life may be related to the temperature of the catalyst bed. As the catalyst life decreases, WABT increases. Figure 8 shows the graph of wabt versus time () used to improve the crude oil feed in the contact zone as described in Figure 1, and curve 136 shows the average WAB Ding pair of the three contact zones. The contact time of the top, middle, and bottom catalysts is about 2 squares. During the operating hours of the large number of hours, the WABT in the contact area only changes,, and C. From the perspective of the relatively stable WABT, the catalyst can be judged. The catalytic activity is not affected. Typically, 3 to 3500 hours of operation at the Zhongmen plant is related to one year of industrial operation. This example shows that crude oil is fed under controlled contact conditions 96 200532010具有 有 t 位 孔 # at least! 8Q A pore size distribution-a catalyst contact and a pore size distribution with a median pore size ranging from ⑽ to i8GA, = the total number of pores in the pore size distribution of at least 60/0 Have holes within the median pore diameter I 巳 of 45 A; additional catalyst contact of U to produce total products containing crude oil products, as determined by p-value, maintains L of crude oil feed / total product mixture ± 1 ± .Ha crude oil product has Reduced TAN, reduced Ni / V / Fe, and reduced the amount of sulphur and oxygen content from the above, and the residue content and VGO content of crude oil products are 90% to 11%. % Of these properties of crude oil feed. One between 90 黾 180 Α contact. Reactor equipment (except for the number and content of _ ρ ^ contact &amp; contact), catalyst formation sulfide method, isolates privacy + heart The method of the product and the method of analyzing the crude oil product are the same as those described in Example 5. A parent catalyst system was mixed with an equal volume of silicon carbide. The crude oil feed to the reactor is described in detail. From the top of the reactor to the bottom of the reactor. The reactor is filled from the bottom to the top in the following way. Carbide is arranged at the bottom of the reactor as a bottom carrier. The catalyst / silicon carbide mixture at the bottom (80 cm3) It is arranged above the Si-Hexite reversed silicon to form the bottom contact area. The bottom catalyst has a median hole and a pore size distribution of 127 A. The total number of holes in the pore size distribution has a pore size within the 32 A median pore size. The bottom catalyst contained ηg of on-mesh and 0.02g of nickel per gram of catalyst, and the remainder was a carrier. The catalyst / silicon carbide mixture at the top (I cm) is configured at the bottom contact 97 200532010

= Into the top contact area. The top catalyst has a median aperture of 1. . A

Middle: 66.7% of the total number of pores in this pore size distribution have a solitary # ^ ^ ° A operation within a median pore size of 20 A. The top catalyst contains 0.003 grams of nickel and 0.12 grams of molybdenum per gram of catalyst, and the mountain is filled above the first contact area with ^ emulsified 1 Lu 1 fossil evening system configuration, filled two positions and used as Hot zone. The catalyst bed garment, 111 is called a furnace, and includes four heating zones corresponding to a preheating zone, two contact zones, and a bottom carrier.

The BS-4 crude oil (Venezuela) with properties summarized in Table 2, «9, was supplied to the top of the reactor. The crude oil feed flows through the preheating zone of the reactor, the H zone of the feedstock and the bottom carrier. The crude oil feed is contacted with each catalyst in the presence of gas. The contact conditions were as follows: the ratio of chlorine gas to the crude oil feed to the reactor was 160 NmVmM (100 SCFB). Is lh, and the pressure is 6.9 MPa (1014.7 psi). The two contact zones were heated to 260 t (500 ° F) and maintained at 260 t (500 τ) for 287 hours. The temperature of the two contact zones was then increased and maintained in the following order: 270 C (525 Τ) for 190 hours, followed by 288 ° c (55 ° C)

216 small day guards, followed by 315 it (6000) 36 hours, then 343. 〇 (650 F) 120 hours to achieve a total operating time of 1173 hours. The total product left the reactor and was separated as described in Example 5. Crude products have an average TAN of 0.42 and an average API specific gravity of 12.5 during processing. This crude product contained 0.0023 grams of sulfur '0.0034 grams of oxygen, 0.441 grams of VGO, and 0.378 grams of residue per gram of crude product. Additional properties of the crude product series are shown in Table 2 of FIG. This example shows that contacting a crude oil feed with pores having a median pore size in the range of 90 to 98 200532010 180 people through a catalyst of a male knife cloth to produce a crude oil product, compared with the properties of the crude oil feed, It has the characteristics of reduced TAN, reduced Ni / V / Fe content, and reduced oxygen content, while crude oil product residue content and VG 0 content are 99% and 100%. fijing &gt; Example 7. Crude oil crude oil ~ ~ contact with catalyst. Reactor equipment (except the number and content of Ramon π a contact), catalyst, total product separation method, crude product eight-block analysis, and catalyst sulfide formation method are as described in Example 6. the same. A crude oil feed (BC-10 crude oil) with properties summarized in Table 3, figure in Q 10, was fed to the top of the reactor. Crude crude oil enters the preheating zone, the top contact zone, the bottom contact zone, and the bottom carrier of the reactor. The contact conditions are as follows: · The ratio of hydrogen to the shoulder supplied to the reactor is 80 NmVm3 (500SCFB) from Liaoyuan / Longjin, LHSV is 2 Ir1, π Moshangda and Moduli is 6.9 MPa ( 1014.7 psi). The two contact zones were gradually heated to 343. ", King C (650 F). The total operating time is 1007 hours. The crude product has an average TAN of 0.16 and an average AH specific gravity of 162 during processing. This crude product contains! 9 wtppm _, 6, nano, 0.6 wtppm The crude product and the unloading of 3 ㈣. The crude product contains 33 g of sulfur, G.002 g of t, 0376 g of VGO, and 0.41 g of residue in the crude oil product of crude oil. Crude oil The products are additionally listed in Table 3 of Figure 10. "This example shows that a crude oil feed is contacted with a selected catalyst having a pore size distribution in the range of 90 to A to produce a crude product, which has a lower TAN, The individual properties of crude oil feeds are 99 200532010 sulfur content, VGO content and residue content of crude oil products of 76%, 94% and ι03%. tExamples 8 to 11 .__ Contact of the palatal system under various contact conditions. The parent reaction apparatus (except for the number and content of contact zones), each catalyst-forming sulfide method, each total product separation method, and each crude oil product analysis system are the same as those described in Example 5. Unless otherwise stated, all catalysts were mixed with silicon carbide in a volume ratio of 2 parts silicon carbide to 1 part catalyst. The crude feed flow through each reactor is from the top of the reactor to the bottom of the reactor. The silicon carbide system is arranged at the bottom of each reactor as a bottom carrier. Each reactor has a bottom contact zone and a top contact zone. After the catalyst / silicon carbide mixture was placed in the contact area of each reactor, the silicon carbide system was arranged above the top contact area to fill the voids and serve as a preheating area for each reactor. Each reactor was fitted with LindbergM, which included four heating zones corresponding to a preheating zone, two contact zones, and a bottom carrier. In Example 8, the uncalcined molybdenum / nickel catalyst / silicon carbide mixture was arranged in the bottom contact area. The catalyst contained 0.146 g of per gram of catalyst and 0.047 g of per gram of catalyst. And 〇21 grams of scale, the rest is alumina support. A molybdenum catalyst / silicon carbide mixture (12 cm3) containing a catalyst having a pore size distribution with a median pore diameter of 180 A was arranged in the top contact area. The molybdenum catalyst has a total content of 0.04 g of molybdenum per gram of the catalyst, and the remainder is a carrier containing at least 0.50 g of alumina per gram of the carrier. In Known Example 9, the unburned # 目 / 明 catalyst / carbonized carbide mixture (4 8 100 200532010 ⑽3) is arranged in two contact areas. The uncalcined platinum / catalyst contains 0.1 g of gadolinium, (MM3 g of mythium, and gallium of phosphorus, and the rest is an alumina carrier. Key catalyst / carbonized carbide mixture (12 cm3 ) Is arranged in the top contact area. The molybdenum catalyst is the same as that in the top contact area of Example 8. In the tenth embodiment, the flip catalyst system and silicon carbide described in the top contact area of Example 8 are used. Mix and arrange in two contact areas (60cy). In Example 11, the uncalcined molybdenum / nickel catalyst / silicon carbide mixture (48 cm3) was placed in the bottom contact ridge. The unwrought The burned turning / recording catalyst contains 0.09 grams of pins per gram of catalyst, 0.25 grams of recordings, and 100,000 grams of scale. The rest is an alumina carrier. Indium catalyst / carbide carbide mixture (12 cm3) is arranged in the top contact area. The rhenium-molybdenum catalyst is the same as that in the top contact area of Example 8. The crude oil from the Mars rig (Gulf〇fMexic〇) is filtered, and then at% ^ (200 F) 'Heated in an oven for 24 hours to generate a crude oil feed having the properties summarized in Table 4, Figure 11 for Examples 8 to 11. = Crude oil feed supply Feed to the top of the reactors of these examples. Crude oil feed is the preheating zone, top contact zone, bottom contact zone and bottom of the reactor. The crude oil feed is in the presence of hydrogen and each catalyst. Contact. The contact conditions of each example were as follows: the ratio of hydrogen to the crude oil feed during the contact was 160 Nm3 / m3 (1_SCFB), and the total pressure of each system was ㈠ MPa (1014 · 7 PS1). During the first 200 hours, the LHSV was 2.0 hours, and then the remaining contact time LHSV was reduced to i 0. The temperature of all contact zones was 343 ° C (650 T) for 500 hours of contact. At 50001 200532010 hours After that, the temperature of all contact zones was controlled as follows: the temperature of the contact zone was raised to 354 C (670 ° F) and kept at 354 ° C for 200 hours; it was raised to 3 66 C (690 F) and kept at 366 ° 200 hours at C; rose to 371.0 ° (700 F) '1000 hours at 371 ° C; rose to 385 ° (725 F) 2000 hours at 3 8 5 C; then rose to 3 9 A final temperature of 9 ° C (750) was maintained at 399 ° C for 200 hours to achieve a total contact time of 23,000 hours. Crude oil products are regularly analyzed to determine the TAN, the hydrogen absorption p-value of the crude oil feed, the VGO content, the residue content, and the oxygen content. The average values of the properties of the crude oil products produced in Examples 8 to 11 are shown in head U. Table 5. "A graph showing the P value (" P ") versus the operating time (" t ") of the crude oil products of each system in Examples 8-11. The crude oil feed has at least 5: binary I-curves 140, 142, 144, and # 146 means that the crude oil feed is individually connected to the four _ systems of Examples 8 to n to the original I oil product? value. For the contact system of the embodiment, in the case of reaching 23,200 hours, most of the cases η, most of the remaining is at least for implementation, and the P value of the running time is greater than 1.5. At the end of Example 2p3: i :) ', the P value is M. The crude product from each test remained fairly stable (e.g., the crude oil feed in τ was maintained during the contact example! Medium: value 1 separation). As shown in Figure 12, in addition to the value ^ added, the ρ value of the crude oil product remained fairly constant in each test. In Big 4 Figure 13 is a graph showing the net hydrogen of crude oil feed for four catalyst systems in the presence of hydrogen. The curves i48, i50, ⑴, 154 represent the net uptake of hydrogen obtained by contacting the crude oil feed individually with each of the catalysts of Examples 8 to u. The net uptake of hydrogen from the crude feed is in the range of 7 to 48 SCFB during a 2,300-hour operation. As shown in Figure Ώ3, the net uptake of hydrogen from the crude feed was fairly constant in each experiment.

Fig. 14 is a graph showing the residual content ("R") of crude oil products as a percentage of the weight of each catalyst system of Examples 8 to "&quot; versus operating time (" t "). In each of the four tests, the crude oil product had a residue content of the crude oil feed with a residue content of 88 to 90%. Curves 156, 158, 1M, and 162 show the residual content of the crude oil product obtained by bringing the crude oil feeds individually into contact with the catalyst systems of Examples 8 to η. As shown in Figure 14, the residual content of the crude oil product remained comparable in most of the experiments.

Fig. 15 is a graph showing the change in API specific gravity of crude oil products ("ΔΑΡΙ ,," versus operating time ("t") for each catalyst system of Examples 8 to u. The crude oil feeds were individually contacted with the catalyst systems of Examples 8 and 11 and the Aρm specific gravity of the crude oil products. In each of the four tests, each crude oil product had a viscosity in the range of 58.3 to 72 7 c. Each The crude oil product's Aρ specific gravity increased by $ 4.1 degrees. The increased API specific gravity corresponds to the API specific gravity of crude oil products in the range of 21.7 to 22.95. The APF specific gravity in this range is ιι0 to Η? The API specific gravity of the crude oil feed. Figure 16 shows the oxygen content of the crude oil product expressed in terms of weight percent 103 200532010 for each catalyst system of Examples 8 to 11 in pores (0 2) versus operating time (' The curves of 172, 174, 176, and 178 in the 矣 -μ mountain & π 8 series show that the crude oil obtained by contacting the catalyst system of the crude oil feed individually = Examples 8 to U Product lice content. Each crude product has an oxygen content of at most "% of the crude feed. Each crude oil product had an oxygen content per gram of crude oil production during each test period. The content should be in the range of M to 0.015 g. As shown in Figure 16, the oxygen content of the crude product remained fairly constant after a contact time of 纟 hours. The relatively constant oxygen content of the crude oil product shows a reduction in the selected organic oxygen compounds during the contact. Because TAN is also reduced in these examples, it can be concluded that at least -fractionate-reactive acid-containing oxygenated compounds have a more selective reduction than non-acid-containing organic oxides. In Example 11, the reaction conditions were 371. It (700 MPa pressure is 6.9 MPa (4.7 psi), and the ratio of hydrogen and crude oil feed was two (1 SCFB), based on the weight of the crude oil feed. The reduction in crude oil feed content was 17.5% by weight. At a temperature of 399 ° C (750 ° F), the same pressure and the ratio of hydrogen and crude oil feed, the crude oil feed MCR was calculated based on the weight of the crude oil feed. The reduction of the content was 25 · 4 wt%. In Example 9, the reaction conditions were: 371 (700 卞), Su Li force was 6.9 MPa (1014 · 7 psi), and hydrogen and crude oil were fed. The ratio is ^ / (1000SCFB), based on the weight of the crude oil feed, the reduction in crude oil feed content is 17_5 wt%. At the temperature of 399 ° C (750 ° F), the same pressure and hydrogen and At the ratio of crude oil feed, the reduction in MCR content of crude oil feed was 19 wt% by weight of crude oil feed. The increase in these reductions in the MCR content of crude oil feed was shown to be uncalcined. Metal barrier catalysts are more capable of reducing MCR content at higher temperatures than unburned metal barrier catalysts 6 and 9. These examples show that TAN (〇8 @ TAN) crude oil feed in contact with-or multiple catalysts to produce crude oil products while maintaining the stability of the crude oil feed / total product mixture and having a net absorption of a relatively small amount of hydrogen = ° selected crude oil products The identity of the crude oil feed with a maximum of 70% is negative. At the same time, the selected properties of the crude oil product are within the same range of the crude oil feed of 20%. Specifically, as shown in Table 4, each t Crude oil products are produced by the net absorption of hydrogen from crude oil feeds up to NmW (275 SCFB). Such products have crude oils with an average TAN of up to 4% of the crude oil feed and an average total Ni / v content of up to 61%. The total Ni / V content of the feed, while maintaining the P value of the crude oil feed above 3. The average residue content of each crude oil product is '88 to 90% of the residue content of the crude oil feed. Each crude oil The average VGO content of the product is VG0 content of the crude oil feed of 115 to 117%. The average API specific gravity of each crude oil product is the Aρι specific gravity of the crude oil feed of 11 to 117%, and each crude oil product has the highest viscosity Viscosity of 45% crude oil feed. 'Example 1 2 to 14 · Original In the case of Huaixie 1, the pore size distribution with a median of at least "j〇A is shocking. In Examples 12 to 14, each reactor device (except the number and content of contact areas) and each catalyst formed sulfur. The physical method, each total product separation method, and each crude oil product analysis system are the same as those described in Example 5. All catalyst systems are mixed with an equal volume of silicon carbide. Crude oil feed stream 105 200532010 per reactor From the top of the reactor to the bottom of the reactor. The silicon carbide system is arranged at the bottom of each reactor as a bottom carrier. Each reactor contains a contact zone. After the catalyst / silicon carbide mixture was placed in the contact area of each reactor, the lithogranite system was arranged above the top contact area to fill the voids and serve as a preheating area for each reactor. Each reactor was charged into a Lindberg furnace, which included three heating zones corresponding to a preheating zone, a contact zone, and a bottom carrier. The crude oil feed was contacted with each catalyst in the presence of hydrogen. The catalyst / silicon carbide mixture (40 cm3) is arranged above the silicon carbide in a shape and contact area for the catalyst system of Example 12 as described in Example 2 and the catalyst is used for the catalyst system of Example 13. The molybdenum catalyst prepared as in Example 3 was used in the catalyst of Beishi Example 14 as the molybdenum / vanadium catalyst prepared in Example 4. The contact conditions of yoke examples 12 to 14 are as follows: Hydrogen and supply to the reactor] The original feed ratio was 160 Nm3 / m3 (100 SCFB), the LHSV was 1, and the pressure was 6-9 MPa (ΐ〇 14.7 psi). The contact zone is gradually heated to 343 ° C (650 T) during a period of time and maintained at 343 t; the next 20 hours, to reach a total operating time of 36 hours. _ Total product_ Contact zone and isolated as described in Example 5. The 12 gate system ’sets the net uptake of hydrogen per catalyst system. In the example, the 'Yin absorption of hydrogen is -10 · 7 Nm3 / m3 (· 65 SCFB), and the crude oil product has a τ Δ Μ-7 Λ' of 6 · 7 5. In Example 13, the net absorption of hydrogen was in the range of 2.2 to 3.0 Nm3 / m3 (13 A • to 18.7 SCFB), and the crude oil product had a ^ 7 &amp; 0.3 to 0.5 ; TAN inside. In Example 14, when crude oil was in contact with indium / catalyst, and L contacted, the net absorption of hydrogen was from _〇.05 Nm3 / m3 to 106 200532010 crude oil product 0.6 NmVm3 (-0.36 SCFB to 4.0 SCFB) has a tan in the range of 0.2 to 0.5. From the point of view of the net hydrogen absorption during the contact period, it is estimated that during the contact between the crude oil feed and the catalyst, the hydrogen system will start with! The rate is 0.7 Nm3 / m3 (65 SCFB). The hydrogen generation during the contact time and the amount of hydrogen used in the conventional process, x allows the use of less hydrogen in the process to improve the properties of poor crude oil f. Contact: The need for less hydrogen will tend to reduce the cost of processing crude oil. In addition, the contact of the crude oil feed with the molybdenum / vanadium catalyst is to produce a crude oil product having a TAN lower than the TAN of the crude oil product produced by the catalyst alone. 15 ^ 1S __ Each reactor equipment (except the number and content of contact zones), each catalyst sulfide formation method, each total product separation method, and each crude oil product analysis system are the same as those described in Example 5 . Unless otherwise stated, all catalysts are paired with 2 sets of carbides! The volume ratio of the catalyst is mixed with the carbide. The crude oil feed flow of each reaction 1 is from the top of the reactor to the bottom of the reactor. An anthracite fossil is arranged at the bottom of each reactor as a bottom carrier. Each reactor has a bottom contact zone and a top contact zone. After the catalyst / carbonite mixture was placed in the contact area of each reactor, the silicon carbide was placed above the top contact area to fill the voids and served as a preheating area for each reactor. Each reactor is housed in a Lindberg furnace and includes four heating zones corresponding to a preheating zone, two contact zones' and a bottom carrier. In each example, the catalyst was prepared as described in Example 2 and used with an additional catalyst. 107 200532010 In Fang's yoke example 15, the additional catalyst / silicon carbide mixture (45 cm3) is used in the bottom contact area. The additional catalyst is the surface catalyst prepared by the method described in Example 3. The catalyst / carbon fossil evening mixture (15 cm3) was placed in the top contact area. '〖16' An additional catalyst / carbonized carbide mixture (30 cm3) is arranged in the bottom contact area, and the additional catalyst is an indium catalyst prepared by the method described in Example 3. The Hungry Catalyst / Carbonite Mixture (30⑽3) was placed in the contact area of the sheet. In Example 17, the 'additional catalyst / silicon carbide mixture (30 cm3) was arranged in the bottom contact area. The additional catalyst was the molybdenum / vanadium catalyst prepared in Example 4. A vanadium catalyst / silicon carbide mixture (3 () cm3) is placed in the top contact area. In Example 18, Pyrex® (Glass works Corporation, New York, U.S.A.) beads (30 cm3) were arranged in each contact area. Crude oil (Santos Basin, Brazil) having the properties summarized in Table 5 and Table 17 for Examples 15 to 18 was fed to the top of the reactor. Crude oil feeds flow through the reactor's preheat zone, top contact zone, bottom contact zone, and bottom carrier. The crude feed is contacted with each catalyst in the presence of hydrogen. The contact conditions for each example are as follows: the ratio of hydrogen to crude oil feed to the reactor was 160 Nm3 / m3 (1000 SCFB) for the first 86 hours and 80 Nm3 / m3 (500 SCFB) for the remaining time period , LHSV is 1 h · 1, and pressure is 6.9 MPa (1014.7 psi). The contact zone is gradually heated to 343 ° C (650 ° F) over a period of time and maintained at 343 ° C to achieve a total operating time of 1400 hours. 108 200532010 These examples show that in the presence of a hydrogen source, crude oil feed and a fifth metal catalyst with a pore size distribution with a median pore size of 35G A are combined with pores with a median pore size in the range of 250 to 300 A. Bayu, a, knives, additional catalyst contact to produce crude oil products, which have changed properties compared to the "like properties" of crude oil feeds, and other properties of the crude oil products, There are only small changes in the same properties. In addition, a relatively small amount of hydrogen uptake from the crude feed was observed during the feed. Specifically, as shown in Table 5, and FIG. 17, the crude oil products of Examples 15 to 17 have tan of a crude oil feed having a TAN of at most 15%. Compared with the same properties of the crude oil feed, the crude oil product produced in Example Η = 1 has a total content of 44% of Fe / Fe, a maximum oxygen content of 75%, and a viscosity of A 75%. . In addition, the crude oil products produced in Examples 15 to 17 have API gravity of a crude oil feed having an API gravity of 100 to 103%, respectively. In contrast, the viscosity of the crude oil product and crude oil feed produced under non-catalytic conditions (Example 18) # Αρι Specific Gravity Phase &amp; produces products with increased occupancy and reduced API specific gravity. From increasing viscosity and decreasing A &quot; specific gravity, it can be concluded that coking and / or polymerization of the crude oil feed has been initiated. Contact of materials at various lhsν. The contact system and the catalyst system are the same as those described in the sixth embodiment. The crude feed, 1 ', is listed in Table 6 in Figure 18. The contact conditions were as follows: the ratio of hydrogen to the crude oil feed to ~ was 160 Nm3 / m3 (1000 SCFB), the pressure was 6.9 MPa (1014.7 Psi), and the temperature in the contact zone was 371 X: (700 F ) To reach the total operating time. In Example 19, the LHSV during the contact period was increased from 1 h- 丨 to 12 h in the course of time, and maintained at 12 h-] at 48 ′ ^, and then increased to 20.7 h · 1, Hold at 20.7 h · 1 for 96 hours. Fang and Beiyuan Example 19 'Analyze crude oil products to determine TAN, viscosity, density, vG0 content, steroid 3 content, heteroatom content, and organic content during the time periods when LHSV is 1 2 1Γ1 and 20.7 h 1 The metal in the form of an acid metal salt is contained. The average values of the properties of the crude oil products are shown in Table 6 and Figures 8-8. ^ As shown in Table 6, Figure 18, the crude oil product of Example 丨 9 has a reduced TAN and a reduced viscosity compared to the TAN and viscosity of the crude oil feed, and the crude oil product has an ApI specific gravity of 104 to 110% of the crude oil. Apl ratio of feed

The weight ratio of heavy MCR i to C: 5 asphaltene content is at least i · 5. The sum of MCR 3 and C5 asphaltene content is lower than the sum of MCR content and c5 asphaltene content of crude oil feed. From the reduction of the weight 2 of the MCR content and the C5 asphaltene content, and the reduction of the sum of the MCR content and the q asphaltene, it can be inferred that the components that have a tendency to form coke will be reduced by bitumen. Crude oil products also have the same total content of potassium, sodium, zinc, and magnesium, and 60% of the crude oil feed is the same. The crude product has a sulfur content of 80 to 900 乂, and the sulfur content of the crude feed is appealing. Examples 6 and 19 show that the contact conditions can be controlled so that lhsv through the contact zone is greater than ⑺ ^ compared to a process with lHSV of 1 h "to produce crude products with similar properties. The ability of k to change the properties of the crude oil feed at liquid space velocities greater than ⑺ h allows the contact method to be performed in a container that is smaller in size than a commercially available container. The smaller container size allows the treatment of inferior crude oil to be carried out at production sites with size restrictions (eg offshore facilities 110 200532010). The contact system and the catalyst system are the same as those described in the sixth embodiment. A crude oil feed having the properties listed in Table 7 of Fig. 19 was added to the top of the reactor and contacted with two catalysts in the presence of hydrogen to produce crude oil products. The two contact zones operate at different temperatures. The contact conditions of the top contact zone are as follows: the temperature of the top contact zone is 丨; the temperature of the top contact zone is 26G ° C (° F); the ratio of hydrogen to crude oil feed is 16〇NmVW ⑽SCFB); and the pressure is 6 9 coffee (ι 〇ΐ4 7 ㈣. The contact conditions in the bottom contact zone are as follows: · The LHSV is 〖h ·〗; the temperature in the bottom contact zone is 315 ° C (_); the ratio of hydrogen to crude oil feed is Nm / m (1〇〇 〇SCFB); and the pressure is 6 9 Mpa ㈣). Eight total products leave the bottom contact area and are introduced into a gas-liquid separator. In the gas-liquid separator, the total product is separated into crude oil products and gases. Crude oil products are regularly Analyze to determine the TAN and C5 asphaltene content. The average value of the properties of the crude oil products obtained during operation is shown in Table 7, = 19. The crude oil feed has 9. ^ ⑽ and A asphaltene content: 0.055 in the oil feed Grams of C5 asphaltenes. Crude oil products have an average content of = AN and C5 asphaltenes of 0.39 grams of c5 asphaltenes per gram of crude oil products. The crude asphaltenes have a maximum asphaltene content of q% of crude oil. C5 asphaltene content of the feedstock. The total potassium and sodium content in the crude oil product is up to 4 53% of the crude oil feed. : Total sum of jade genus. The TAN of the crude oil product is at most 10% of the crude oil into the spoon of TAN. The p value is maintained at 15 or higher during the contact. 111 200532010 As shown in Examples 6 and 20, it has a low The contact temperature in the second (bottom in this example) zone is 50. The first (top in this example) contact temperature tends to make the q lff content of the crude oil product better than the c asphaltenes of the crude oil feed. The content is more reduced. In addition, the use of a controlled temperature difference will reduce the metal content of the organic acid metal salt form. For example, r, in each embodiment, has the stability of a crude oil product mixture with a fixed phase. (E.g. p㈣ tester)

In the following, the total potassium and sodium content of the crude product of Example 20 was reduced more than the total potassium and sodium content of the crude product of Example 6. The first contact zone using pure temperature can tolerate high molecular weight compounds (such as C5 asphaltenes and / or organic acid metal salts), which will have compounds that form polymers and / or have physical properties that are soft and / or sticky (Such as gum and / or 'oil). Removal of these compounds at lower temperatures is removed before they become clogged and catalyzed, thereby: configuring the catalyst lifetime to operate at higher temperatures behind the brother-contact zone. --W W Catalyst contact

The bulk metal catalyst of this application and / or the catalyst (100 grams of catalyst = 0 side to 5 grams or 002 to 4 grams of catalyst in the material) can be suspended in crude oil in some cases And the reaction under the following conditions: degrees in the range of 85 to 425 ° C (085 to 797 T), pressure in the Mo &amp; range to 10 MPa, and the ratio of hydrogen source and crude oil feed is 16 to 1 (A period of time. The crude oil product is separated at a reaction time sufficient to produce the crude oil product using separation equipment such as a transitional device and / or centrifuge, mediator and / or residual crude oil feed. Crude oil product and crude oil feed phase 112 200532010 may It has altered TAN, iron, osmium, fen / bucket, zl and reduced C5 ^ snails, and / or vanadium content. Asphaltene content. Those skilled in the art should further modify and substitute for the appearance of bad things in this specification. Each of the x: means: ... to achieve the purpose of teaching two terms: :: r λ and method. It should be understood that the form of the present invention can not be expressed and described in the m: Examples of examples. Can replace several pieces and materials illustrated and described in this article 'can reverse parts and procedures of the present invention , May be used alone

Certain features of the invention, all of which are described at Wangkou, after obtaining the benefits of the description of the present invention 'should be apparent to those skilled in the art. Changes may be made in the elements described herein without departing from the spirit and scope of the invention as described in the appended claims. [Brief description of the drawings] For the technical person who is eager to learn the drawings, the advantages of the present invention having the following detailed description will become apparent after referring to the drawings, where: Figure 1 is a specific example of a contact system Simple diagram. Figures 2A and 2B are simplified diagrams of a specific example of a contact system including two contact areas. 3A and 3B are diagrams showing a specific example of a contact system including three contact areas. Fig. 4 is a schematic diagram of a specific example of a separation zone incorporating a contact system. Fig. 5 is a schematic diagram of a specific example of a blending zone of a contact system. Figure 6 is a diagram of the specific example of the combined separation zone, contact system, and blending zone. Fig. 7 is a list of representative properties of crude oil processing and crude oil products for specific examples of the crude oil feed tray: a specific example of the contact of catalysts and catalysts. Fig. 8 shows a crude oil feed tray. Or the weighted average ± the specific example of catalyst contact, the graph of the urine / m degree versus the running time. Figure 9 is a specific example of the contact between crude oil feed and two catalysts. 'Figure 10 is another list of the representative properties of crude oil and crude oil with two kinds of crude oil feeds, two specific examples of contacting feed tanks, Shanli this, and An Touch. Figure Π is the crude oil feed and A list of the four specific crude oil feeds and crude oil products contacted by the four example J catalyst systems. Figure 12 is the specific real crude oil products that brought the crude oil feed into contact with the four example 4 ^ j catalyst systems. The graph of P value vs. running time. Example Γ3 is the specific drawing of the net absorption of hydrogen from the oil feed to the running time of the specific crude oil feed in contact with four different catalyst systems. Residues of crude oil products in feed and four different catalyst systems, expressed as weight percentages Content vs. transportation: Graphical representation of the time. Tianqian s on the operating time example: 15 is the API gravity ratio of crude oil products in which the crude oil feed is brought into contact with four different catalyst systems. Graphical representation of the operating time Fig. 16 is a diagram showing the crude oil product Λ, expressed as a percentage by weight, when the crude oil feed is brought into contact with four different catalyst systems. The graph of the operating time in the milk is the specific example of the crude oil feed that contacts the catalyst system Examples of crude oil 114 200532010 List of representative properties of feed and crude oil products. The catalyst system contains various amounts of flip catalyst and sharp catalyst, and catalyst systems containing thallium catalyst and flip / sharp catalyst, and glass beads. Figure 18 is a list of properties of crude oil feeds and crude oil products for specific examples of contacting crude oil feeds with catalysts at various liquid space velocities. ~ Figure 19 is a specific example of contacting crude oil feeds at various contact temperatures. List of properties of crude oil feeds and crude oil products. The invention allows for various modifications and alternative forms, but its specific specific system. It is not possible to draw pictures without scale. You should understand its diagrams and details. The description is not # — Wu A is not used to limit the present invention to the specific forms &lt;, but on the contrary, it is intended to cover the spirit and scope # within the scope of the patent application as appended. 7 Ί W ^ Modifications, equivalents, and substitutions [Description of main component symbols] 100: contact system 102: contact area 104: conduit 106; conduit 106 ... conduit 108: separation area 110: conduit 112: conduit 11 4: contact area 11 6: Contact zone 115 200532010 1 18: Catheter 120: Separation zone 122: Catheter 124: Catheter 126: Catheter 128: Catheter 130: Blend zone 132: Catheter 134: Catheter # 136: Weighted average bed temperature (WABT) vs. operating time Curve 140-146: P value of crude oil product versus operating time curve 148-154: Net absorption of hydrogen versus operating time curve 15 6-162: Residual content of crude oil product versus operating time curve 164-170: crude oil Product API gravity vs. running time curve 172-178: Oxygen content of crude oil product vs. running time • 116

Claims (1)

200532010 X. Scope of patent application: 1 · A method for producing crude oil products, the crude oil feed is made with one or more of the total products including: where the crude oil products are in contact to produce a mixture containing crude oil products, the crude oil feed Contains 5. 〇 and 〇.101 Mpa are liquid metal salts, one or more organic acids, one or more test compounds of two organic acids, the crude oil is fed per gram of the alkaline earth metal hafnium, or mixed organic There are at least 0.00001 grams of metals in the test of the acid metal salt form. There is at least 0.00001 grams of catalyst in each gram of catalyst, with gold i / total content containing 篁 's at least grams of: gen reset meter' contains at least please! One or more of the present gels in Table 6 and one of the six in the Periodic Table ^ one or more compounds of multiple metals, or a mixture thereof; and The contact conditions are controlled so that the liquid space velocity in the contact zone exceeds the industrial hl, so that the crude oil product has an alkali metal and an alkali in the form of an organic acid metal salt. The content of alkali metals and alkaline earth metals, among which the alkali name and alkaline earth metals in the form of metal salts of organic acids are determined by ASTM method D1 3 1 8. 2_ The method according to the scope of patent application, wherein the total content of alkali metals and alkaline earth metals in the form of organic acid metal salts in the crude oil product is at most 50%, at most 10%, or at most 5% of the crude oil feed Alkali and alkaline earth metal content in organic acid metal salt form. 3. The method according to item 1 of the scope of patent application, wherein the total content of alkali metals and alkaline earth metals in the form of organic acid metal salts in the crude oil product is from 丨 to 80%, 10 to 70%, 20 to 60%, or 3 0 to 50% of the crude oil feed 117 200532010 in the form of organic acid metal salt alkali metal Gion duplex Meng belongs to the range of summer. 4. According to the method of any of the items in the scope of applying for a patent, the crude oil product contains gram of crude product per gram of crude product from gram to gram to gram. 0.00000 gram, or from the genus 100,000. M, 1 gram of organic acid metal salt in the form of metal test and earth test-5. If the scope of the application for a patent (any of the-method), one or more of the metals in 1 is molybdenum and / or tungsten. —6. The metallurgical medium according to the method of any one of the scope of applying for a patent… has a pore size distribution with a median pore size of at least ㈣, at least μ, or 1 80 Α. Μ 7. If a patent is applied for The method of any one of the scope of ..., wherein the catalyst further comprises one or more metals in column 5 of the periodic table, one or more compounds of one or more metals in column 5 and one or more metals on the periodic table, One or more compounds of one or more metals in columns 7 to 10, and / or mixtures thereof. 8. The method according to any one of claims 1 i 7 in the patent application scope, wherein 6 metal catalysts In addition, one or more compounds of the 15th block of the periodic table—or one or more elements and 7 or one or more elements of the 15th block. Xi—9. The method according to any one of the claims 1 to 8 in which —Or the catalysts additionally include additional catalysts which have a median ^ at least A pore size distribution of 60A or at least 80A. The method according to any one of claims 1 to 9 in which the crude oil feed is brought to a contact zone located or connected to offshore equipment Intermediate contact 118 200532010. π-inches are determined according to any one of items 1 to ϋ, and intermediate contact includes contact in the presence of a hydrogen source. "12. Methods such as applying item η in the scope of patent applications Among them, the 'δ' Hai crude oil feedstock absorbs molecular hydrogen at a selected rate to suppress contact / phase separation of the crude oil feed. &Quot; 丨 During contacting, if any of the scope of applications for patents i to 12: any method: the method still includes The crude oil product is combined with the crude oil feed phase = its crude oil to form a blend. It is obtained by a method of any one of items 1 to 13 of different I4 · -type crude oil products or blends. ^ No. 1 in the scope of patents 5. —A method for producing fuels and products for transportation ', which includes the addition, use of fuel, lubricating oil or chemicals or blends. To make the crude product or blend , France '· 17 wherein the processing comprises as patent wide range of the partial} or hydrotreating process comprising a 16 1 of the process XI Circular: page 119 such as hypophosphorous