TW200533738A - Systems and methods of producing a crude product - Google Patents

Abstract

Contact of a crude feed with one or more catalysts produces a total product that includes a crude product. The crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed. The crude product is a liquid mixture at 25DEG C and 0.101 MPa. One or more properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed. In some embodiments, gas is produced during contact with one or more catalysts and the crude feed.

Description

200533738 IX. Description of the invention: [Technical field to which the invention belongs] The present invention relates generally to systems and methods for processing crude oil feeds, and, for example, to compositions made using such systems and methods. In more detail, the specific examples described herein are related to the conversion of the crude oil feed with a residual content of ".2 g of residue to a rhenium liquid mixture at 25. 〇 and 〇 :; 〇1 Mpa, and ⑻One or more systems and methods of crude oil products that have improved properties compared to the same properties of the crude oil feed. [Prior art], the possibility of being unsuitable or unsuitable for the purpose of allowing crude oil to be economically transported or Crude oils processed using traditional facilities are often referred to as disadvantaged crudes. ~ Inferior crudes often contain relatively high levels of residues. Such crudes are often difficult to transport and / or process using conventional facilities. And expensive. High-residue crude oil can be converted to coke after high temperature treatment. Alternatively, high-residue crude oil is usually treated with water at high temperature to produce a less viscous crude oil and / or crude oil mixture. During processing, the use of known Means may be difficult to remove water from the unlucky crude oil and / or crude oil mixture of the father. Inferior crude oil may contain hydrogen deficient hydrocarbons. In Canada When working with depleted hydrocarbons, it is usually necessary to add a consistent amount of hydrogen, especially if unsaturated fragments are generated due to the cracking process. Hydrogenation during processing usually involves the use of active hydrogenation catalysts, which may require suppression of unsaturated fragments Coke formation. Hydrogen production and / or transportation to processing facilities is very expensive. 200533738 Coke can quickly form and / or deposit on the catalyst surface during inferior crude oil processing. To regenerate contaminated coke The catalytic activity of the catalyst can be very high. The high temperature used during regeneration may also weaken the catalyst or degrade the catalyst. Inferior crude oil may contain the total acid value ("TAN" / T! 11 π ^? &Quot; τ ΑΝ " ^ ^ ^ ^ ^ ^ / or cause the metal components to rot during processing. Removal of acidic components from inferior crude oil may include chemically neutralizing the acidic components with various bases. Or Use of anti-corrosion surname metal in transportation equipment and / or processing equipment. The use of anti-corrosion rhymes usually involves considerable costs, so the use of anti-corrosion equipment may be unsatisfactory. Another method of tank suppression : Add corrosive agents to 'grade crude oil' before shipping and / or processing of inferior crude oil. The use of rotten name inhibitors may adversely affect equipment used to process crude oil and / or products made from the crude oil W Inferior crude oils may contain relatively high amounts of metal contaminants, such as nickel, Syria, and / or iron. During processing of such crude oils, metal contaminants and / or compounds of metal contamination may be deposited in contact with On the surface of the catalyst or on the void volume of the catalyst: Such deposits can cause low catalyst activity. Inferior crude oil usually contains organic-bonded heteroatoms (such as sulfur, oxygen and nitrogen). Organic-bonded heteroatoms In some cases, it may have a negative effect on the catalyst. Metal test salts and / or soil test metal salts have been used in the process of residue desulfurization. These procedures are prone to lead to poor desulfurization efficiency, to produce poor oil-insoluble demetallization efficiency, formation of a substantially inseparable salt-oil mixture, use of a large amount of hydrogen, and / or a relatively high hydrogen pressure. 200533738 Some methods to improve the quality of crude oil include adding diluents to inferior crude oils to reduce the weight percentage of ingredients that cause inferior properties. However, the addition of diluents often increases the cost of processing inferior crude oil because of the cost of the diluent and / or the cost of managing the inferior crude oil. Adding diluents to inferior crudes can in some cases reduce the stability of such crudes. The following US patent cases: 3,136,714 to Gibson et al; 3,558,747 to Gleim et al; 3,847,797 to pasternak et al; 3,948,759 to King et al; 3,957,620 to Fukui et al; 3,960,706 by McCollum et al; 3,960,708 to McCollum et al; 4,1 19,5 28 to Baird, Jr. et al; 4,127,470 to Baird, Jr. et al; and Fujimori to the Nets 4,224,140; 4,437,980 to Heredy et al .; 4,5,91,426 to Krasuk et al .; 4,665,261 to Mazurek; 5,064,523 to Kretschmar et al .; 5,166,118 to Kretschmar et al .; 5,288,681 to Gatsis; 6,547,957 to Sudhakar et al .; and US Patent Application Publication Numbers: 20030000867 to Reynolds and 20030149317 to Rendina, describing various methods and systems for processing crude oil. However, the methods, systems, and catalysts described in this patent also have limited utility due to the many technical issues mentioned above. In short, inferior crude oils generally have undesirable properties (e.g., relatively high residues, a tendency to corrode equipment, and / or a tendency to consume a significant amount of nitrogen during processing). Other undesirable properties include relatively high levels of unwanted components (eg, relatively high TANs, organically bonded heteroatoms, and / or gold 200533738 contaminants). il-like properties have been fragrant + # μ Tobes are problematic in traditional transport and / or processing facilities' including increased cooking benefits.v., corrosion resistance, reduced catalyst life, and / or during processing Increased use of hydrogen. Therefore, there is a clear economic and technical need for improved systems, methods, and / or catalysts for converting inferior crude oil into crude products with more desirable properties. SUMMARY OF THE INVENTION The invention described herein generally relates to a system and method for contacting a crude oil feed with a catalyst to produce a complete product containing crude oil products and, in some specific examples, non-condensable gases. The invention described herein also relates generally to a composition in which Gu Ru # 八 ^, 〃 T has a novel combination of ingredients. Such compositions can be obtained by using the systems and methods described herein. Ben: A method for preparing a crude oil product is provided, which comprises contacting a crude oil feed and a source in the presence of a plurality of catalysts to produce a crude oil product, wherein one or more of the catalysts include catalyst. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a lice source in the presence of one or more catalysts to produce a complete product comprising the crude oil product, wherein the crude oil product is at 25. . And 0.101: Pa is a liquid mixture, at least one of the catalysts contains one or more transition claw compounds, and the crude oil feed has an amount of crude oil per gram of crude oil = ::: ㈣, as determined by a -3.7. J * pieces so that the crude oil product contains at most 0 () 5 per gram of crude oil product, and the crude oil product contains at least 0. Shekel " per gram of crude oil product, and the light oil has at least An octane number of 70. The present invention also provides a method for preparing a crude oil product, which comprises: contacting a 200533738 crude oil feed with a hydrogen source in the presence of a hydrogen source or a medium to produce a complete product including the product, ° HAI crude product at 25. (: With 0.11 metal sulfide, at least one of the catalysts contains-or more transitions and the beta crude oil feed has a content of at least 02 grams per gram of crude oil feed: as measured by cafa_7 ...: The crude oil product includes coal and oil, and the kerosene is per kilogram of the household, and the crude oil product contains at most 0.05 g of coke per gram of crude oil product. 3 The invention also provides a method for manufacturing a crude oil product, Including: contacting a crude oil feed with a hydrogen source in the presence of-or a plurality of catalysts to produce a complete product comprising a crude oil product, wherein the crude oil product is between 25 and 0.11

Mpa is a liquid mixture, at least one of the catalysts contains-or more transition metal sulfides', and the crude oil feed has a residual content of at least 0 2 2 per gram of crude oil feed; and controlling the contact conditions such that the crude oil product Each gram of crude oil product contains at most 0.05 grams of coke 'wherein the weight ratio of atomic hydrogen to atomic carbon in the crude oil product is at most K75' as determined by the astm method DO. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of one or more catalysts to produce a complete product comprising the crude oil product, wherein the crude oil product is between 25 and 0.

Mpa is a liquid mixture, at least one of the catalysts contains one or more transition metal sulfides, and the crude oil feed has a residue content of at least 0 2 ^ 200533738 residues per gram of crude oil feed, the center of the butter oil feed = = 7, and the reset ratio of the original flight to the atomic slave (H / c) is under the control condition 'make the crude oil product be the atom'

The ratio of 80-120% of the original + Η / Γ μμ ^ 坭 卄 atomic H / C, from the feed M oil product has a maximum of 30% residue content of the crude oil, as determined by the crude oil 吝私 # — 士 π υ: > όΌ / ', the system mother gram original> The product contains at least 0.001 g of light oil, and the light oil has an octane number of at least 70. The present invention also provides a method for manufacturing a crude oil product, and comprises contacting a material and a gas source in the presence of one or more catalysts to produce a complete product contained therein, wherein the crude oil product is at 25 V 〇⑻: 二 :: 体 组合 物, At least one of the catalysts contains-or more transition metal compounds, and the crude oil feed has a residual content per gram of the original residue, as determined by the ASTMW test; with j = Shu conditions, the crude oil product is per gram. The crude product contains: at least ..001 = the light oil has a scorch value of at least 7G; at least 0 · g grams of the plant:,: Haier kerosene contains aromatic compounds' the kerosene is less than U grams of aromatic compounds per gram of coal , As measured by ASTM method _86, and: "The oil has a freezing point of at most, the temperature, the rule of 6 households is measured; at least 0.001 grams of vacuum gas oil (v =: each * VG0 contains at least · 3 grams of aromatic compound, as measured by P method 368/90; and at most

Assayed by Method D5307. Gram of stubble, such as ASTM, the present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of-or a plurality of catalysts containing transition metal sulfide catalysts 200533738 to make leather The complete product of the crude oil product 5 is a liquid mixture at 25 ° C i η 1 Λ1 Λ / Γ ”into 庶 //, 0 · 101 MPa, the transition h 'mother gram total transition metal sulfide The catalyst contains a total of or at least one transition metal sulfide, and the crude oil is fed with a residual content of 0.2 grams of residue per gram of crude oil, ^ ASTM method = 307; and the contact conditions are controlled so that The crude oil product contains at most 0.05 g of coke per gram of crude oil product, and the crude oil product has at most

Reverse the ten slaves, check the residue content of 30%, as determined by the astm method D5307.

This wool month also provides a method of manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of one or more catalysts including a transition metal sulfide catalyst to produce a complete product including the crude oil product, wherein The crude product was 纟 25. (: The mixture is a liquid mixture at Xiao 010 MPa. The transition metal sulfide catalyst contains at least 0.4 grams of one or more transition metal sulfides per gram of total transition metal sulfide catalyst. The feed has a nitrogen content of up to 0.001 grams of nitrogen per ^ of crude oil, and the crude feed has at least 0.2 {residue residue content per gram of raw material / raw material; and control contact conditions so that the crude oil The product has at most 3 of the nitrogen content of the crude feed, and the crude product has a residue content of at most 30% of the crude feed residue content, where the nitrogen content is as determined by the astm method, and the residue The content is as determined by ASTM method D5307. The present invention also provides a method for manufacturing a crude oil product, comprising: subjecting a crude oil feed and a hydrogen source in the presence of one or more catalysts containing a transition metal sulfide catalyst Contact to make a complete product containing crude oil products, where the 11 200533738 crude oil product is at 25. (: with o.ioi Mpa is a liquid mixture, the transition metal sulfide catalyst contains per gram of total transition metal sulfide catalyst contains Total At least 0.4 grams of one or more transition metal sulfides, the crude feed has a total Ni / V / Fe content of at least 0.0001 grams of Ni / V / Fe per gram of crude feed, and the crude feed has per gram of crude Feed at least 0.001 g of residue, and control the contact conditions so that the crude oil product contains up to 0.05 g of coke per gram of crude oil product, and the crude product has at most Ni / V for the crude oil feed Total Ni / V / Fe content of 90% of Fe / Fe content, the crude oil product has a residue content of at most 30% of the crude feed feed residue content, wherein the Ni / V / Fe content is as determined by ASTM method D5863 The residue content is as determined by ASTM method D5307. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in one or more catalysts containing a transition metal sulfide catalyst; Contact in the presence of a medium to produce a complete product containing crude oil products, where the = oil product is a liquid mixture at 25 and 0.001 Mpa, and the transition metal sulfide catalyst is per gram of total transition metal sulfide catalyst Contains one or more of up to /0.4 g Transition metal sulfide, the crude oil is fed and has a sulfur content of 0.001 g of sulfur per oil, and the crude oil feed has a residual content of at least 0.2 gram of slag in the crude oil feed, And controlling the contact 铩 =, it is obtained that the crude oil product has a residue content of at most 70% of the sulfur content of the crude oil feed, and the crude oil product has a residue content of at most the crude oil feed residue content <刈%, of which sulfur The content is as measured by ASTM method D4294, and the residue content is as measured by ASTM method D5307. The invention also provides a 12 200533738 method for manufacturing a transition metal sulfide catalyst composition, which includes: oxidizing the transition metal And a metal salt to form a transition metal oxide / metal salt mixture; reacting the transition metal oxide / metal salt mixture with hydrogen to form an intermediate; and the intermediate and sulfur in the presence of one or more hydrocarbons Reaction to produce a transition metal sulfide catalyst. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of one or more catalysts including a transition metal sulfide catalyst to produce a complete product including a crude oil product, wherein the Crude products are at 25. (: It is a liquid mixture with 0.101 Mpa. The transition metal sulfide catalyst contains transition metal sulfides. The crude oil feed has a residue content of at least 0.2 grams of residue per gram of crude oil feed, as determined by ASTM method D5307. Control the contact conditions so that the crude oil product has a residue content of up to 30% of the crude oil feed residue content; and wherein the transition catalyst is obtained as follows: a transition metal oxide is mixed with a metal salt, To form a transition metal oxide / metal salt mixture; react the transition metal emulsion / metal salt mixture with hydrogen to form an intermediate; and make the physical reaction in the presence of or in the presence of hydrocarbons to produce a transition Metal sulfide catalyst. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of-or a plurality of catalysts to produce a complete product comprising the crude oil product, wherein the crude oil product At 25 and (M01 P |, the liquid is this compound ', and the crude oil feed contains grams of dross per gram of crude feed as determined by ASTM method D5307; Where the whole product is made into vapour; at 25. (: cooled with 0.101 Mpa 13 200533738 at least a part of the vapour is condensed; and a crude oil product is formed, wherein the crude oil product is a mother gram crude oil product containing at least 0.001 g Light oil, which has a scorch value of at least 70; at least 0.001 g of VGO, the VGO master gram VGO contains at least 0.3 g of aromatic compounds, as described in the IP method 368/90 Testers, and residues of up to 0.05 g, as measured by asTM method D5307. The present invention also provides a method for producing a crude oil product, comprising: making a crude oil feed and a hydrogen source exist in an inorganic salt catalyst Contact to produce a total product containing a crude oil product, wherein the crude oil feed has a residue content of 0.2 grams of residue per gram of crude oil feed, as determined by method "D5307" The crude oil product is a liquid mixture at 25 ° C and 0.11 Mpa, and the crude oil product contains at least 0.001 grams of light oil per gram of crude oil product, and the light oil contains up to 彡 0 · per gram of light oil. 0.001 g of monocyclic ring aromatic compound Baxter by ASTM method D6 730 measured; at least 001 grams of Gu effluent 'and up to 0.05 grams of residue, as measured by ASTM method D5307, the present invention also provides a method for manufacturing crude oil products, comprising: The feed is contacted with a hydrogen source in the presence of an inorganic, Olympian catalyst to produce a complete product containing crude oil product, i / h methylamine, from feed to feed with gram crude oil to 0.2 g residual 〉 Check residues> Check content As measured by ASTM method D5307, the crude oil product is a liquid mixture at 25 ° C 0101 _ m ^. /, · 01 MPa, and the ', ^ products are per gram of crude oil The product contains the first 3 people, at least 0.001 grams of diesel, and 4 wood oil per gram of diesel contains up to

,earth. r υ · 3 g of the square compound, as measured by the IP method 368/90; at least Wang Xi 〇〇001 g of VG, and the VGO line 14 200533738 as ^ method 368/90 ASTIVT method j ) 5307 female grams of VGO contain at least the tester; and at most the tester. 0.3 g of aromatic compound and 0.05 g of residue, as also provided by the present invention-a method for producing a crude oil product, a crude oil feed is contacted with a hydrogen source in the presence of an inorganic salt catalyst to produce; including: making oil The complete product of the product, where the crude oil product is a liquid mixture under the original conditions, the crude oil feed has a content of ~ g gramme, such as _faca 7 = at least u crude oil feed has per gram of crude oil feed It is expected that the monocyclic cyclic aromatic compound content of at most 01 and 50 may be controlled; and that the aromatic compound is controlled to have at most G.2 grams at 25 grams per gram of crude oil feed during the contact period. ^, So that non-condensable hydrocarbons are formed at MP :, as determined by mass balance: 1: make crude oil products have at least 5% w eight deniers containing W-'° generous, crude oil into early ring-ring aromaticization : Human I: ':: Group compound content' wherein the monocyclic ring aromaticization &amp; substance-containing stem system is as measured by ASTM method D673. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product including a crude oil product, wherein the crude oil product is at 2 "c: 〇i 〇i: pa is a liquid mixture, the crude oil feed has a residue content of at least 0.2 grams of residue per gram of crude oil feed, as determined by the astm method 05307, and the crude oil feed has The olefin content expressed in grams of olefins; and controlling the contact conditions such that the crude oil product has an olefin content of at least 5% greater than the lean smoke content of the crude feed, where the olefin content is as determined by the aSTM method D6730. 15 200533738 The present invention A method of manufacturing a crude oil product is also provided, comprising: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product comprising a crude product, wherein the crude product is at 25 ° (: 0.101) Liquid composition under Mpa 'The crude oil feed has a residue content of at least 0.2 grams of residue per gram of crude oil feed, and the inorganic salt catalyst exhibits a temperature of between 50 ° C and 500 ° C. The turning point of the exhaust gas in the range of exhaust gas, as determined by the Temporal Analysis of Products (TAP) and the control of the contact conditions, so that the crude oil product has at most a residual content of the crude oil feed <30% The residue content is based on the "chuck number table" of the crude oil product per gram of crude oil product, wherein the residue content is as determined by ASTM method D5307. The invention also provides a method for manufacturing a crude oil product, comprising: The crude oil feed is contacted with a hydrogen source in the presence of an inorganic salt catalyst to produce a 70-king product containing the original product, where the crude oil product is a liquid mixture at 25 ° C and 0.101 Mpa. In the case of at least 0.2 g / y, the inorganic salt catalyst contains at least two kinds of inorganic metal salts, and the inorganic salt catalyst exhibits an exhaust gas turning point of exhaust gas in a temperature range, such as the instantaneous analysis of the product. # (TAP) The tester, wherein the temperature range of the turning point of the discharged milk is in the DSC temperature of at least one of the two inorganic metal salts, and η _ the DSC of the inorganic salt catalyst. Between temperatures; and control of contact conditions, the crude oil product has a residue of at most 30% of the crude feed residue content, which is based on the residue of each gram of crude oil product. The number of grams in the table tf is the same as that determined by the μ method. The present invention also provides a method for inserting and producing crude oil products, which includes: 16 200533738 crude oil feed and hydrogen source. Helmet extinction, contact in the presence of a salt-forming catalyst to complete the product of the synthesizing oil product, the I in the basin is ◦3, P-eight &amp; Hai crude oil product at 25 ° c and 0.101 Mpa Erguang "The crude oil feed has at least 02 per gram of crude oil feed, and the radon content of the residue is' as measured by ASTM method d53q7. The natural catalyst shows that the catalyst is between 50 and 500. The row between the corpse and the temperature range = the body: the gas turning point 'such as the instantaneous analysis of the product (τΑρ = two and ^ crude oil products, so that at 25ec ^ G iGiMp

= :, the volume of the crude oil produced is at least 5% greater than the volume of the crude oil feed. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product comprising a source / source product, wherein the crude product is at 25. 〇 和 〇 · 1 () 1Μρ:

Below is a liquid mixture with this crude oil feed having at least 0 ·: per gram of crude oil feed. Gram of residue, and the inorganic salt catalyst exhibits an exhaust gas turning point of exhaust gas in a temperature range between 50γ and 50 [, as measured by the product mesh 4 knife analysis (TAP); and The contact conditions were controlled so that at most 0.2 g per 25 g of crude oil feed during contact. 〇 and 〇 ι〇ι may form non-condensable hydrocarbons, as determined by mass balance. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product comprising a crude oil product, wherein the crude oil product is at 25 and 001 The liquid mixture is at Mpa, the crude oil feed has a residue content of at least 0.2 g of residue per gram of crude oil feed, and the inorganic salt catalyst has a content of 200. (Thermal transition in the temperature range between ^ and 500 ° C, as measured by differential scanning calorimetry 17 200533738 (Dsc) at a rate of 10 QC per minute; and control of the contact conditions' such that crude oil products have &Amp; 'Chadori', which is at most 30% of the content of the crude oil feed residue, is expressed in grams of residue per gram of crude oil product, where the content of residue is as determined by ASTM method D5307. The present invention also Provided is a method for manufacturing a crude oil product, comprising:

The crude oil feed is contacted with Wuyuan in the presence of an inorganic salt catalyst to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° c and 010 MPa, and the crude oil feed has A gram of crude oil is fed with a residue content of at least 0.2 gram of slag, and the ionic conductivity of the inorganic salt catalyst is at least °, ..., and the inorganic salt in the organic salt catalyst is at least 300. (: To 500. (: ionic conductivity at a temperature in the range; and control the contact conditions so that the crude oil product has a residue content of at most the crude oil feed residue content, which is expressed in grams of residue per gram of crude product , Where the residue content is as determined by ASTM method D5307.

The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a whole product including a crude oil product, wherein the crude oil product

A liquid mixture, the crude oil feed has a residue content of at least 0.2 t of residue per gram of crude oil feed, the inorganic salt catalyst comprises an alkali metal hafnium, wherein at least one of the metal salts is an alkali metal carbonate, And the alkali metal has an atomic order of at least 11 and the at least-atomic ratio of the alkali metal having an atomic order of at least 11 to the alkali metal having an atomic order greater than 11 is in a range of 纟 0 · 1 to 10; and controlling the contact conditions such that The crude oil product has a residual content of at least the content of the crude feed feed check, where the residual content is as determined by ASTM 18 200533738 method D5307. The invention also provides a method for manufacturing a crude product, comprising: contacting a crude feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product, wherein the crude feed has at least 0.2 grams per gram of crude feed In the residue 3 of the residue, the inorganic salt catalyst of Haihai contains an alkali metal salt, wherein the alkali metal salt to ν is an alkali metal hydroxide, and the alkali metal has an atomic order of at least 11 and an atomic order of at least 11 The test for the alkali metal atomic number of 11 is greater than 11: at least-the atomic ratio of the genus is in the range of 0 · 1 i 10; at least the 7 ^ king product of P knife is made into steam; at 25 0C and 0 · ι 〇ΐ Mpa cooling down to a part of the vapor; and the formation of the crude oil product, in which the crude oil has a residue content of 30% of the residue content of the crude oil of Hai Hai. The present invention also provides a method for manufacturing a crude oil product, which comprises: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce complete production; two: a crude oil feed having at least one gram of crude oil feed 0.2 g of residue: slag, the amount of 'the inorganic salt catalyst contains alkali metal rhenium, wherein the alkali metal salt is at least one of metal test hydride' and the metal test has a total I of at least u: to and an atomic order of at least 11 The test metal has an atomic order greater than 11 and the test section 8 6>, an atomic ratio is in the range of 0 · 1 to 10, · at least one product is made into a vapor; ... and the condensate at 0 · 101Mρα has the vapor; And the formation of the crude oil product, which makes the crude oil production ... 30% of the residue content of the crude oil feed residue content. This book "also provides a method of manufacturing crude oil products. ^ Crude oil feed gold_ # • The completion of contacting 4 sources with oil products in the presence of inorganic salt catalysts. 吝 你 * 丄 衣 仏 3 25 ... mixed with 〇 ″ 〇1 Mpa 19 200533738 for liquid mixture, the crude oil feed has at least 0 2 grams of residual content per gram of crude oil feed, the inorganic salt catalyst contains one or more alkali metals Salt,-or multiple alkaline earth metal salts or mixtures thereof, wherein one of the alkali metal salts is an alkali metal carbonate, wherein the alkali metal has an atomic order of at least u; and controlling the contact conditions so that the crude oil product has at most the crude oil feed Residual fish content of 30% of residual fish content, wherein the residual fish content is as determined by method D5307.

The present invention also provides a method of manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product comprising a crude oil product &apos; wherein the crude oil product is at 25. . And 〇1〇 ～ is a liquid mixture, the crude oil feed has a residue content of at least gram of residue per gram of crude oil feed, the inorganic salt catalyst contains one or more alkali metal hydroxides,-or multiple alkaline earth metal salts or A mixture in which the alkali metal has an atomic order of at least 11; and controlling the contact conditions such that the crude oil product has a residue content of at most 30% of the residue content of the crude feed, wherein the residual content is as determined by ASTM method D5307 .

Bu Yue Yue also provides a method for manufacturing a crude oil product, which comprises contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product of the product, wherein the crude oil product is at 25. (: And 0.11) is a liquid mixture, the crude oil feed has a residue content of at least gram of residue per gram of crude oil feed, the inorganic salt catalyst contains one or more alkali metal compounds, one or more alkaline earth metals A salt or a mixture thereof, and wherein the base has an atomic order of at least 1 1; and the contact conditions are controlled so that the raw material has a residue content of at most 30% of the residue content of the crude oil feed, 20 200533738 is based on per gram of crude oil The residual gram number of the product is expressed, wherein the content of the residue is as determined by ASTM method D5 3 07. The present invention also provides a method for producing hydrogen, which includes: crude oil feed and one or more smokes in an inorganic salt The catalyst is contacted in the presence of water, the hydrocarbons have a carbon number in the range of 1 to 6 'the crude oil feed has at least 0.2 H residual content per gram of crude oil feed, and the inorganic salt catalyst exhibits The exhaust gas turning point of the exhaust gas in the temperature range between 500 ° C and 500 ° C, as measured by the product transient analysis (TAP); and the generation of hydrogen. This description also provides a method for producing crude oil products. A method comprising: making -The crude oil feed is contacted with the inorganic salt catalyst in the presence of steam: two gas streams are generated 'the gas stream contains hydrogen, wherein the-crude oil feed has a residue content of at least 0.2 g of residue per gram of the first crude oil feed, such as Those tested using the astm method 053, and the inorganic salt catalyst exhibited an exhaust gas turning point of the exhaust gas in a temperature range between 500c and 5,000, as shown by the product instantaneous two-phase analysis (TAP) Measurer; contact the second crude oil feed with the second catalyst in the presence of at least-part of the generated gas stream to produce a complete product containing the crude product, where the crude product is between 25 ^ and 〇ι〇ι — The following is a liquid mixture; and the contact conditions are controlled so that one or more properties of the crude oil product are changed by at least 10% compared to the respective—or multiple properties of the second crude oil feed. The present invention also provides- A method of gas flow, comprising: contacting a crude oil feed with an inorganic salt catalyst in the presence of steam, wherein the crude oil feed has a residue content of at least 0.2 grams of residue per gram of crude oil feed, such as 卩 21 200533738 ; And production ―A gas stream containing nitrogen, fossil fossils, and carbon dioxide 'and wherein the molar ratio of carbon monoxide to carbon dioxide is at least 0.3. The present invention also provides a method for manufacturing a crude oil product, which includes ... The salt catalyst 'contacts the crude oil feed with a nitrogen source in the presence of the adjusted inorganic salt catalyst' to produce a complete product comprising a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0-101 Mpa, The crude oil feed has a residual content of 彡 0.2 grams of residue per gram of crude oil; and controlled contact with f wood pieces so that the crude oil product has at most 30 / ^ of φ in the residue of the crude oil feed. The slag contains 1, which is expressed as the number of grams of slag per gram of crude product, wherein the slag content is determined by ASTM method D5307. The present invention also provides a crude oil composition comprising a boiling range distributed at 300 ° C. and… at 010 MPa. . ^ ,,. &quot; Hydrocarbons, 4 hydrocarbons include isoparaffins and normal paraffins, where the weight ratio of isoparaffins to normal paraffins is at most 1.4, as determined by ASTM method D6730. The present invention also provides a crude oil composition, each gram of which contains: at least 0 · _g of hydrocarbons having a boiling range distribution of up to 2G4 0c_ (400 ° F) at G.1G1 MPa, at least 0.001 g Hydrocarbons whose boiling range is between 2.04.0 and 300 ° C at 0.1 MPa and at least 0.00 g are distributed at 300 0C and 400 at 0.10 MPa . &lt;: hydrocarbons between, and at least 0.001 g of hydrocarbons with a boiling range distributed between 400 ° C and 538 C (1,000) at 0.101 MPa, and the boiling range distribution is Cigarettes of up to 204 C contain isoparaffins and normal paraffins, where the weight I ratio of isoparaffins to normal paraffins is at most 1.4, as determined by ASTM method D6730. 22 200533738 = Ming also provides a crude oil composition, which contains: grams of light oil per gram of composition, the light oil has an octane number of at least 70, and the light oil is a mother gram light oil containing up to 0. 15 grams of thin smoke, as measured by the ASTM method D6r0; at least 1 gram of emu oil, «oil series contains at least 0.2 grams of aromatic compounds per gram of kerosene, such as those measured by astm &amp; d, and the Kerosene has a freezing point at a temperature of at most _30oc, as measured by ASTM method D 2 3 8 6 and those with a maximum of 0.05 g of residue, as measured by ASTM method D5 3 07 Assessor.

The present invention also provides a crude oil composition, each gram of which contains: 0.15 grams of non-condensable hydrocarbon gas at 25 ° C and 0.1 (1 Mpa), the non-condensable flue gas is per U of condensable hydrocarbon gas Contains up to 0.3 grams of hydrocarbons with a carbon number from 43 (Cl to C3); at least 0.001 grams of light oil with an octane of at least 70; k value, at least G.GG 1 gram of kerosene The kerosene has a freezing point at a temperature of at most _30%, as measured by ASTM method 6, and the kerosene contains at least 0.2 grams of aromatic compounds per gram of kerosene, such as by A · method.

86 testers' and up to 0.05 g of residue, as measured by aStm method D 5 3 07. The present invention also provides a crude oil composition containing per gram of composition: at most 0.05 g of residue, as measured by ASTM method D5307; to. At least 0.001 grams of hydrocarbons with a range of up to 204 ° C (400 F) at 0.101 MPa and at least 0.001 grams of boiling range distribution at 0.101 MPa are collapsed. (: And 300. (: hydrocarbons between :; at least 0.001 g of Fortin range at 0.001 MPa at 300. (: and 400; &lt;: hydrocarbons between; at least The boiling range of o.ool gram at 0.101_3 is distributed between 40.0 and 538.0 (1, 00023, 200533738); and wherein the boiling range is between 2G ° C and 2G4 ° c: cloth :: = Mole ratio of rare hydrocarbons containing terminal double bonds and rare molecules with intramolecular double bonds to olefins with intramolecular double bonds is at least 0.4, as shown in ASTM method D6730 Xiben Moming also provides a crude oil composition, each gram of the composition contains: to the gram residue, as measured by 卩 ASTM * D53〇7; and at least 0. gram stagnation range distribution in 2G Hydrocarbon mixtures between 0 and 538 qc (ι, delete π 'as determined by ASTM &amp; 3 () 7, and the

Each gram of the hydrocarbon mixture contains: at least 100,000 grams of chain smoke, as determined by ASTM * D673〇; at least 100,000 grams of thin smoke,

^ Measured by ASTM method D673q, and the olefins contain v 0.001 grams of terminal olefins per gram of smoke, as measured by the astm method 0673〇; at least 0.0G1 gram of light oil; at least 丨 kerosene The kerosene system has at least 0.2 grams of aromatic compounds per gram of kerosene a. As described in ASTM method D5186, at least 0.001 grams of diesel oil is included. 3 grams of aromatic compounds, as determined by the IP method 368/90; to 0.001 grams of vacuum gas oil (), the VG0 is 0.3 grams of aromatic compounds per gram of VG0, such as Measured by the ip method 368/90. The present invention also provides a crude oil composition, each gram of which contains: at most 0.05 g of residue, as measured by the ASTM method D5307; Warp classes with a boiling range distribution of up to 204 ° C (400F) at 0.101 MPa; at least 0.01 g of hydrocarbons with a boiling range between 204 ° C and 300 ° C at 0.101 MPa; at least 〇〇〇1 g of hydrocarbons with a boiling range between 300 ° C and 400 ° C at 001 MPa 24 200533738; and at least 〇〇〇〇1 gram at Hydrocarbons with a boiling range distribution between 400 and 538 (1,000 0F) at 0.101 MPa, as measured by ASTM method D2887; hydrocarbon systems with boiling ranges up to 204 ° C, boiling range distribution per gram The warp class to 204 C contains: olefins of at least 0.0000 g, as determined by aSTM method D6730; and paraffins of at least 0.001 g, the paraffins containing isoparaffins and normal paraffins, The weight-to-weight ratio of iso-paraffins to normal paraffins is at most 1 · 4, as measured by ASTM method D6730. The present invention also provides a crude oil composition containing 0.05 g of residue per gram of composition, as measured by ASTM method D5307; and at least 0.001 g of boiling range distribution at 0.101 MPa is Up to 2400 (: (400 〇F) hydrocarbons; at least 0.001 g of hydrocarbons with a boiling range between 204.00 and 300 ℃ at 0.001 Mpa; at least 〇00. 1 gram of hydrocarbons with a boiling range distributed between 3000 c and 4,000 at oi MPa; 乂 0.001 grams of boiling range distributed at 400 MPa at 001 MPa. 匸 and 538 hydrocarbons between c (1, 000, 000F), as determined by the ASTM method; and where the boiling range is distributed between] 〇0 (: and # 204% # control type contains carbon number 4 (C4) compound, the C4 compound contains at least 0.001 g of butadiene per gram of C4 compound. The present invention also provides a crude oil composition, which contains 0.50 g of residue per gram of composition, At least 001 g of hydrocarbons distributed in the lower boiling range of at most 仙 ^ ^ ^ ^ 〜 ~ at least ⑴❻ ... grams of boiling range distribution in ^ ⑸ MPa in 204 ℃ and 3〇 Hydrocarbons between plutonium, at least 0.001 g, boiling range at 0.001 MPa, warp types between 3000 c and 4000 c 25 200533738, and at least 0.001] The boiling range of gram is distributed at 400 at 0.101 MPa. (: Guardian between 538 and γ, and one or more catalysts larger than 0 g but smaller than 0.001 g. Catalyst contains at least one or more alkali gold

In some specific examples, the present invention also provides a crude oil feed in combination with one or more of the methods or compositions according to the present invention, which have not been processed, steamed, and / or separated in refineries. It contains a carbon number of 纟 4 or more, and the crude oil feed contains at least 0.5 grams of such components per gram of crude oil feed; (C) contains hydrocarbons, some of which have: , The boiling range distribution at 1GG Y, the boiling range distribution between 100 and 200 ° C at G.1G1 MPa, and the range at 〇i〇i Mpa. c Boiling range distribution between people 3 00 c, boiling range distribution between 3,000 c and 400 ° C at 〇i〇i, and 400 ° C and 700 ° at 〇i〇iMpa Distribution of boiling range between C; (d) Each gram of crude oil feed contains &gt;, 0.001 grams of less than 10,000 ° C boiling range distribution at 0.001 Mpa, at least 0.001 The boiling range is distributed at 100 ° C at 0 ° 〇1 MPa.

For hydrocarbons between 200 ° C, at least 0.001 g has a boiling range of 200 at 0 · 101 MPa. (: Hydrocarbons between 3,000c and at least 0.001g at 0 · 101 MPa, boiling ranges distributed between 300 0c and 400 0C 'and at least 0.001 g at 0.101 MPa Lower boiling range hydrocarbons distributed between 400 C and 700 ° C; (e) has a TAN; (f) 0.2-0.99 g, 0.3-0.8 g, or 0.4-0.7 per gram of crude oil feed Gram of residues; (g) containing zinc, iron, iron, or mixtures thereof; (11) containing sulfur; and / or nitrogen-containing hydrocarbons. In certain embodiments, the present invention also provides a method according to the present invention. 200533738 Hydrogen source of one or more combinations of methods or compositions, which: ⑷ is gaseous; ⑻ contains molecular hydrogen; ⑷ contains light hydrocarbons; ⑷ contains methane, ethane 'propane or a mixture thereof; (e) contains water And / or (f) mixtures thereof. In certain embodiments, the present invention also provides a method in combination with one or more of the methods or compositions according to the present invention, which comprises adjusting the inorganic salt catalyst 'wherein Adjusting the inorganic catalyst includes: (i) heating the inorganic salt catalyst to at least a fan's temperature; and / or (ii) heating the inorganic salt catalyst to 300 ℃ lower temperature and cooling of inorganic salt catalyst at most times.

Degree 0

In some specific examples, the present invention also provides a method in combination with-or more of the method or composition according to the invention, which comprises contacting crude oil 枓 with-or multiple catalysts and controlling the contact conditions: 条件 so that Between contact, there is at most 0.2 g, at most 0.15 g, at most or at most 0.05 g of non-condensable smoke at 25 ° c # 〇1〇1 MPa, as determined by mass balance; (b) making The contact temperature is within the range of 25 ° F or between 260-550; the force is within the dry range of 0 ° F; (d) the ratio of the gaseous hydrogen source to the crude oil feed is per cubic meter; the crude oil feed is 1_161 () () Or 5.32 () within the range of standard cubic meters of hydrogen source; ((乂 suppress coke annoyance generation; ⑺ to suppress the production of coke in the complete product during contact or ^ ^ from the feed, (g) makes The crude oil product has a strength per gram of crude oil product, 0.05 g, at most 0.03 g, at most 0 g, or at most 0. 3: Excessive :: (h), at least a part of the inorganic salt catalyst can be obtained Under such contact conditions: semi-liquid or liquid; ⑴ so that the crude oil product has at most 90% TAN; ⑴ makes the crude oil product have a total Nj / V / Fe content of up to 90%, up to 50% or up to 5% of the Fe content for the crude oil; (k) makes the crude oil The product has a sulfur content of up to 90%, up to 60% or up to 30% of the sulfur content of the crude oil feed; ⑴ making the crude oil product have up to, up to 50%, up to 50% or up to 10% of the nitrogen content of the crude feed. % Nitrogen content; ㈣ makes the crude oil product have a residual content of up to 3G%, at most ⑽ or at most of the residual content of the crude oil feed, ammonia and crude oil products are produced together; ⑷ makes the crude oil product contain A # And the method further comprises: recovering methanol from the crude product, combining the recovered methanol with an additional crude feed to form an additional crude feed / methanol mixture; and heating the additional crude feed / methanol mixture , So that the TAN of the additional crude oil feed is reduced below i; ⑻ :: One or more properties of the crude oil product are changed by up to 9 denier days compared to the individual one or more properties of the crude oil feed—,丨 9, ⑷ make the contact area Catalysts: The total catalyst of Erwei ... 00g crude oil feed ... g; The source of wind is added to the crude oil feed before or during the contact. Fargo has specific wealth, and the present invention also provides and compiles the The contact conditions of one or more combinations include: mixing the inorganic salt catalyst with the crude oil feed at a temperature below _C, and the salt catalyst is substantially insoluble in the crude oil feed-in ~~ inorganic catalyst; And / or make the crude oil = contact in the presence of steam in the crude oil feed to make a complete product containing = inorganic: catalyst in water and / or oil products. The original method of the next A liquid mixture: tr example 'The present invention also provides a method in combination with or in combination with the formula according to the present invention, which comprises contacting the crude oil: 28 200533738 contact with an inorganic salt catalyst and the further steps include: before contacting or Providing steam to the contact zone during the period; (b) forming an emulsion of the crude oil feed and water before contacting the crude oil feed with an inorganic salt catalyst and a hydrogen source; ⑷ spraying the crude oil feed into the contact zone β; and / Or ⑷ contact the steam with the inorganic salt catalyst to remove the surface of the inorganic salt catalyst At least partially remove the coke. In some specific examples, the present invention also provides a method in combination with one or more of the methods or compositions according to the present invention, including contacting a crude oil feed with an inorganic salt catalyst to produce a complete product At least a portion of the complete product is made with steam, and the method further includes condensing at least a portion of the vapor under Naa and 0.ΗΗ Mpa to form the crude product, the contact conditions are controlled such that: (a ) The crude product further comprises a component having a selected boiling range distribution; and / or the rhenium crude product comprises a component having a selected API specific gravity. In certain embodiments, the present invention also provides a method in combination with one or more of the methods or compositions according to the present invention, comprising contacting a crude oil feed with one or more catalysts and the one or more catalysts It is non-acidic. In certain embodiments, the present invention also provides K3Fe] Si4 catalysts or transition metal sulfur catalysts in combination with one or more of the methods or compositions according to the present invention. K5Fe per gram] s "catalyst or transition metal sulfide catalyst contains a total of at least 0.4 g, at least 0.6 g, or at least 08 g of at least one transition metal sulfide; (b) at We]; the catalyst or transition metal sulfide catalyst The atomic ratio of transition metal to sulfur in the medium is in the range of 02 to 20; further comprising-or more alkali metals, one or more alkali metal-or more compounds or mixtures thereof; further comprising- Or more than one soil test 29 200533738 metal, one or more compounds of an alkaline earth metal or a mixture thereof; further comprising one or more alkali metals, one or more compounds of an alkali metal or mixtures thereof, wherein the catalyst or The atomic ratio of the transition metal to sulfur in the transition metal sulfide catalyst is in the range of 0.5-5_2, and the atomic ratio of the test metal to the transition metal is in the range of 0 to 1; (f) further includes One or more bases The atomic ratio of transition metal to sulfur in the K3Fei () Si4 catalyst or transition metal sulfide catalyst is a metal or one or more compounds or mixtures of alkaline earth metals or a mixture thereof; The atomic ratio of the alkaline earth metal to the transition metal is in the range of 0 to i; (g) further contains zinc; (h) further contains; ⑴ further contains KFeS2; and / or ⑴ is non-acidic. In some specific In an example, the present invention also provides a combination with one or more of the methods or compositions according to the present invention, wherein the K3Fe10S14 catalyst is formed on the spot. In some specific examples, the present invention also provides a method or One or more transition metal sulfides in combination of one or more of the compositions, or in which: (a) contains one or more transition metals selected from 6 to 10 of the periodic table, and one or more selected from 6 to 6 One or more compounds or mixtures of transition metals in column 10; (b) containing one or more iron sulfides; (c) containing FeS; (d) including § FeS2, (e) a mixture containing iron sulfides, wherein the Iron sulfide is based on the chemical formula Fe (id) s Indicate that it is within the range of 0 to -17, (f) further comprising after contact with the crude oil feed; (g) at least one of the transition metals of the one or more transition metal sulfides is iron And / or (h) is deposited on a support, and the transition metal 30 200533738 sulfide catalyst contains up to 0.25 g of total support per 100 g of catalyst. In some specific examples, this The invention also provides a transition metal sulfide contact in combination with one or more of the methods or compositions according to the invention

A method for forming a medium composition, the method comprising mixing a transition metal oxide with a metal salt to form a transition metal oxide / metal salt mixture; reacting the transition metal oxide / metal salt mixture with hydrogen to form an intermediate; and The intermediate reacts with sulfur in the presence of one or more hydrocarbons to produce a transition metal sulfide catalyst: (a) the metal salt comprises an alkali metal carbonate; 0) it further comprises dispersing the intermediate in one or more In liquid hydrocarbons, they are simultaneously reacted with sulfur; (c) wherein one or more of the hydrocarbons have a boiling point of at least 1000c, (d) wherein one or more of the hydrocarbons are vg0, xylene Or a mixture thereof, (e) wherein mixing the transition metal oxide and the metal salt includes mixing the transition metal oxide and the metal salt in the presence of deionized water to form a wet paste; making the wet paste at a temperature ranging from 150-250 Drying; and calcining the dried paste at a temperature ranging from 300-600; (f) wherein reacting the intermediate with sulfur includes heating the intermediate to a range from 240-350 in the presence of at least one of the hydrocarbons(: Temperature; and / or (g) it further comprises contacting the catalyst composition with a crude oil feed comprising a source of sulfur and hydrogen.

In some specific examples, the present invention also provides an inorganic salt catalyst in combination with one or more of the methods or compositions according to the present invention, which comprises: (a) or more alkali metal carbonates, one or more tests Earth metal carbonates or mixtures thereof; (b)-one or more alkali metal hydroxides, one or more alkaline earth metal hydroxides or mixtures thereof; (c) one or more alkali metal hydrides, one or more alkaline earth metal hydrides Or its mixtures; (d) one or more alkali metal (s) 31 200533738 sulfide, one or more sulfides or mixtures of one or more earth test metals; (e) —one or more acids of metal test Amines, one or more ammonium amines or mixtures thereof; (f) one or more metals selected from Block 6-10 of the Periodic Table, one or more selected from Box 6-10 of the Periodic Table (G) —or more than one inorganic metal salt, and at least one of the inorganic metal salts generates a hydride '· (h) sodium, potassium, rhenium during the use of the catalyst , Planer or mixtures thereof, ⑴ calcium and / or magnesium; ⑴ sodium A mixture of salt and potassium salt, and the potassium salt comprises potassium carbonate, potassium hydroxide, potassium hydride or a mixture thereof, and the sodium salt comprises sodium carbonate, sodium hydroxide, sodium hydride or a mixture thereof; and / or (k) its mixture. '. In some specific examples, the present invention also provides an inorganic salt catalyst containing an alkali metal in combination with one or more of the compounds according to the present invention, (2) (a) an atomic number of at least 11 The atomic ratio of the alkali metal to the alkali metal having an atomic order greater than 11 / Λ T 'is in the range of 0.1 to 4; (b) the atomic ratio of at least two to: sodium: potassium in the alkali metal is in °, 1 Within the range of 4; (:) the atom of the unloading pair ^ two, unloading, and nano-unloading, nano-opposite and at least three ^ ^ in the range of 0.1 · 5; (d) the alkali metal The neutron ratios are in the range of 0 potassium and hammer, and the original potassium, planed, and fine of sodium to potassium, sodium to absolute, and potassium to hammer; ⑷ at least three of the alkali metals are in the range of 5 And the atomic ratios of internal discharge, absolute discharge, and conical heterogeneity are each in some publication methods or compositions. The present invention also provides the media according to the present invention, and U) Combination of inorganic salts containing carrier materials &amp; materials include oxidized oxide, oxidized oxide, magnesium oxide, oxygen 32 200533738 hydrated hydrotalcite, oxidized oxide, oxidized oxide, iron oxide, oxidized lock, oxidation: φ :: Syria, antimony oxide or mixtures thereof; and / or thorium incorporated into the support material are:-or more metals selected from the 6-10th column of the periodic table, and metals selected from columns 6-10 of the periodic table One or more compounds; one: a variety of carbonates,-or more metal hydroxides, one or more alkali to lice compounds, one or more alkaline earth metal carbonates, one or more alkaline earth metal hydroxides , One or more alkaline earth metal hydrides and / or mixtures thereof.

In some specific examples, the present invention also provides a method in combination with one or more of the methods or compositions according to the present invention, #including contacting a crude oil feed with an inorganic salt catalyst, wherein: The catalyst activity of the catalyst is substantially unchanged in the presence of sulfur; and / or the inorganic salt catalyst is continuously added to the crude oil feed. In some specific examples, the present invention also provides an inorganic salt catalyst in combination with one or more of the methods or compositions according to the present invention, which exhibits a (4) turning point of the exhaust gas in the TAP temperature range, and the The exhaust gas contains water gas and / or carbon dioxide; (b) thermal transition in the temperature range between 200.500, 250-450 ℃, 300-400, such as differential scanning calorimetry. Per minute. (: Heating rate measured; (c) DSC temperature in the range of 2000-500 or 25 0-450. (:); (d) at a temperature of at least 100, A broader X-ray diffraction pattern than the x-ray diffraction pattern of the inorganic salt catalyst below 1000; and / or ⑷ after adjustment, the ionic conductivity at 3000c is smaller than that of the inorganic salt The ionic conductivity of the catalyst before adjustment. In some specific examples, the invention also provides a method according to the invention 33 200533738

_ -V- of the method or composition; ^ ^, A combination of inorganic salt catalysts in the temperature range, the temperature range of the exhaust furnace Yunke 丄 τ /, Chen Xiong at _ 4 discharge turning point, as TAP Institute The tester also determined the contact conditions such that the contact temperature was 1 or higher, which means that the TAP temperature of the inorganic salt catalyst was 300 c or 20 m below the TAP temperature. ^ ； ^ At TAP temperature or at 1 LV μ · β / bucket, γ ^ ′ (b)

U is above it and / or ⑷ at least the TAP &gt; degree of the inorganic salt catalyst. In some specific examples, the present invention also provides an inorganic salt catalyst in combination with one or more of the methods or compositions according to the present invention, which or among them ... at least at the TAp temperature of the inorganic salt catalyst is Liquid or semi-liquid, and the dream inorganic salt catalyst is at least the TAp temperature ^ Xiao TAP temperature is the minimum temperature at which the inorganic salt catalyst exhibits a turning point of exhaust gas; (b) in the range from 50. A temperature of 0 to 50 ° C is a mixture of a liquid phase and a solid phase; and / or at least one of the two inorganic salts has a DSC temperature above 500 ° C. In some specific examples, the present invention also Provide an inorganic salt catalyst in combination with one or more of the methods or compositions according to the present invention, which, when tested in the form of particles that can pass through a 1000 micron filter, will be heated to a temperature of at least 0 ° C when Self-deformation under gravity and / or under a pressure of at least 007 Mpa 'causes the inorganic salt catalyst to change from the first state into the second form, and the second form is cooling the inorganic salt catalyst to 20 degrees. (: Can not be changed back to this first form. In some specific examples, the present invention also provides an inorganic salt catalyst in combination with one or more of the methods or compositions according to the present invention. The medium contains: at most 0.01 g of bell or bell compound, which is based on lithium 34 200533738, η-, (b) up to 0.001 g of halide, which is based on the weight of halogen; and / or at most 0.0001 grams of a glassy oxide compound. In some specific examples, The invention also provides a method of the present invention or composition - the product completely or be combined with, per gram of product was completely έ at least 0.8 grams of crude product.

In some specific examples, the present invention also provides a crude oil product in combination with one or more of the methods or compositions according to the present invention, which contains at most G.GG3 g, at most 0.02 per gram of crude oil product. Grams, at most Q Q1 grams, at most 0.05 grams, at most 0_001 grams, at least 0_grams, at least 0.005 grams or 0.00G1-G.G 3 grams of residue; ⑻ per gram of crude oil The product contains coke from 0 g to 0.05 g, 0.0001 g to 0.003 g, or 0000 g to 001 g; ⑷ has an olefin content of at least 10% greater than the olefin content of the crude feed; (3 per gram of crude oil product 3 has a total inorganic salt catalyst greater than 0 g but less than 0 0 J g, as determined by mass-to-mass balance; (e) each gram of crude oil product contains at least 0. 0.99 g, 0.04-0.9 g, 0_0.8 g of VG; ⑺ contains VGO and the VG0 system contains at least 0.3 g of aromatic compound per gram of VG;

(g) s has 0.001 grams or 01_0 5 grams of crane effluent; ⑻ at most atomic H / C, ⑴ has 9% of the crude oil feed H / c] 10% of atoms with less than 10% The content of monocyclic ring aromatics in the crude oil feed is early cyclic ring aromatics; (k) monocyclic ring aromatics including dibenzobenzene and ethylbenzene f ethylbenzene compounds; ⑴ per gram The crude product contains up to 0.1 g of benzene, 0.05-0.50 g of toluene, 0.3-0.9 g of m-xylene, 0.5-0.15 g of ortho containing at least 0.0001 g or -toluene and 0.2- 0.6 g of para-xylene; (m) 0.01-0.5 g of diesel oil; (n) containing diesel oil, 35 200533738, and the diesel system contains at least 0 001 $ per .3 grams of diesel oil per gram of diesel oil. Private compounds; (〇) contains 801 grams, from 0 to 0.7 grams or 0 001 · 0 (P) contains kerosene, and Xizhan, Shan and A Shi Jian spoon kerosene, ης Α δ HAI kerosene system The mother gram of kerosene contains at least 0.2 grams or at least 0.5 grams of aromatic compounds, and / or coagulation or vortex points at temperatures of up to fC, and (q) contains at least 0.001 grams or at least 0.5 grams of light oil; (R) Package _ n ^ 工 'In light oil series, each gram of light oil contains at most 0.01 Ϊ to 205 grams or at most 2 grams of benzene, at least 70, at least 80 = a scorch value of 2 and / or Chain-burning smoke and n-hydrocarbons, where isoparaffin vs. normal-chain burning hydrocarbons in the oil I is at most 1.4; and / or (s) /, up to> 10% greater than crude oil feed Volume by volume. In some specific examples, the present invention also provides one or more groups of methods or compositions according to the present invention. 7 methods' which include contacting a crude oil feed with a catalyst to form A complete product of the crude product, the method further comprising: (i) combining the crude product with a crude oil that is the same or different from the crude feed to form a blend suitable for transportation; (b) combining the crude product with A crude oil that is the same or different from the crude oil feed is combined to form a blend suitable for processing design; (c) the crude oil product is left over, and (d) the crude oil product is fractionated into-or A variety of venues and manufacture transportation fuel from at least one of the venues; and / or when the catalyst is a transition metal sulfide catalyst, process the transition metal sulfide catalyst so as to remove the transition metal sulfide catalyst The catalyst recovers metal. In certain specific examples, the present invention also provides a crude oil product in combination with one or more of the methods or compositions according to the present invention, each gram of crude oil product contains: at least 0.001 g of VGO, and the The VG〇 series contains at least 0.3 grams of aromatic compounds per gram of vG〇; ⑻ at least 0.001 grams of diesel oil, 36 200533738, and the diesel series contains s per gram of diesel oil, and the main compound is 0.3 grams less. At least 0.001 grams of light oil, namely, earth; 1; 1 This light oil: Each gram of light oil contains at most 0.5 grams of the original, at least 70 oxine, benzene, and / or isoparaffin and normal paraffin, Wherein, the iso-paraffin to n-paraffin ratio is at most 1.4; (d) a total of /0.001 g / furten range distribution is at most 204 (such as 0. 〇)

7-knife mixture ', and the mixture is based on ene smoke per gram of mixture; ⑷ the weight ratio of atomic hydrogen to atomic charcoal in the composition is at most 175 or at most U; ⑴ at least 0 · _g of kerosene, and The kerosene contains at least 0.5 grams of aromatic compounds per gram of kerosene and / or has a freezing point at a temperature of at most -30 ° C; (g) from 13 to 13 grams of atomic hydrogen per gram of composition; ⑻ Non-condensable hydrocarbon gas and light oil 'When combined, it contains at most 0.15 grams of olefins per gram of combined non-condensable flue gas and light oil; ⑴ Non-condensable hydrocarbon gas and light oil, when combined, contains isoparaffin and normal oil Paraffinic hydrocarbons, where in the combined light oil and non-condensable hydrocarbon gas, the weight ratio of isoparaffins to normal paraffins is at most 14; hydrocarbons having a carbon number of up to 3 include: carbon number 2 (Co and 3 (C3) alkenes and paraffins, and the weight ratio of the combined I and I olefins to the combined dagger and q alkane is at most 0.3; the olefins and paraffins of carbon number 2 (C2), where I olefins are c: 2 paraffins have a weight ratio of at most 0.2; and / or olefins and paraffins having a carbon number of 3 (C3), where the weight of q olefins to q paraffins is Having a butadiene content of at least 0.005 grams (K);; ratio of at most 5.3 billion billion) has 15.5. API specific gravity in the range of 15 to 30 hours; (妁 has a total Ni / V / Fe of up to 0.00001 grams per gram of composition; (11) the paraffin content of hydrocarbons with a boiling range distribution of at most 204 is 0.7- Within 0.98 grams; (0) hydrocarbons with a boiling range of up to 204 ° C, with a boiling range of 37 200533738 hydrocarbons with a distribution of up to 204 ° C, containing 0 Λ c + · · · 5 grams of fluorene ( p) The distribution of boiling range of olefin-containing hydrocarbons is at most 205 D, ±, C, and the dilute olefin contains at least 0.001 g of terminal sclerotium, and (q) contains the distribution of olefin boiling range. For hydrocarbons up to 204 ° C, Η # π, ^ is negative and the olefin has a molar ratio of terminal olefins to dilute hydrocarbons of at least 0 4; and / or ⑴ per gram at 20 °. Tobacco ⑼〇〇ιι_0.5 grams of hydrocarbons in the distribution range of the inter-boiling range. Broken In certain embodiments, the present invention also provides a combination of one or more of the methods or compositions according to the present invention. Crude oil product containing at least one of the catalysts containing one or more alkali metals, wherein (a) at least one of the alkali metals -Which is a bell, a fine or planer, or a mixture thereof; and / or at least one of the catalysts-further comprising a transition metal, a transition metal sulfide, and / or limonite: bartonite. -In the specific example, the characteristics from a specific specific example of the present invention may be combined with the characteristics from other specific examples of the present invention. For example, the characteristics from a specific example may be combined with the characteristics from any of the other specific examples. Combining. Crude oil products are obtained via any of the specific and further specific examples, methods, and systems described herein that can be described herein. In further specific examples, additional features are added to the examples. [Embodiments] Detailed description of the invention Here, some specific examples of the present invention will be described in more detail. The terms used in this article 38 200533738 are defined as follows. "Metal test" is used as a deduction ^ ', said one or the evening selected from the first table of the periodic table The metal, one or more compounds selected from the periodic table # 1, M ^ "/ Table 1 metal or one or more compounds or their mixed" alkaline earth metal "means one or more selected from the periodic table One or more compounds selected from metals in column 2 of the periodic table, metal or metals in column 2 or their AMU "means atomic mass units." ASTM "means American Standard Tests and Materials Can Qin d φ

TestlngandMaterials).

"Cs asphaltene" means asphaltenes that are insoluble in pentane. C5 asphaltene content is as measured by ASTM method D2007. Crude oil feed, crude oil products, light oil, kerosene, diesel and VGO's, hydrogen peroxide Specific gravity and atomic carbon percentage are as measured by the astm method, API specific gravity refers to the specific gravity of Aρ at 15.50 ° C. Specific gravity of Aρm is as measured by the ASTM method 06822. Unless otherwise mentioned, the boiling range of crude oil feeds and / or complete products = distributions are as obtained by ASTM method D5. Hydrocarbon components, such as bonds- The content of hydrocarbons, isoparaffins, olefins, naphthenes and aromatic compounds in light oil: as determined by AS ™ * D673〇. The content of aromatic compounds in wood oil and VG〇, such as Described by IP method 368/90. Aromatic 39 200533738 Amount is as measured by ASTM method D5186 (Bronsted-Lowry acid) refers to the molecular body that has this force. Containing `` Bronister-Rorrowine in kerosene to another molecular body by quinone-rory base '' refers to the ability to accept 1-body Bronister-Rorry base from another molecular body. Examples of tests include hydroxy (OH) (water (H2O)), carboxylate (RCO "), halide (Br—, C1, F, 1), hydrogen sulfate (HS〇4-), and sulfate ( SO /-). The number of carbons refers to the total number of carbon atoms in the molecule.… The carbon system means that the solid coke containing system contains carbonaceous solids that do not vaporize under the conditions of the method, as determined by mass balance. Coke Weight is the total weight of the solid minus the total weight of the input catalyst. Each mile refers to the weight of a component in the matrix (such as crude oil feed, complete product or crude product), expressed as a weight fraction or Percent by weight. "Wtppm" means parts per million expressed by weight. "Diesel" refers to a boiling range distributed between 26 ° and 343 ° C (500-650 ° C) at 0.101 MPa. Hydrocarbons. The diesel content is determined by the astm method D 2 8 8 7. The "distillate" system Hydrocarbons with a boiling range between 204 and 343 ° C (400-650 ° C) at 0.101 MPa. The distillate content is as determined by ASTM method D28 87. The distillate may contain kerosene and diesel "DSC" refers to differential scanning calorimetry. "Freezing point" and "freezing point" refer to the temperature at which crystalline particles form in a liquid. The freezing point is as measured by ASTM D2386. 40 200533738 GC / MS '' system Refers to gas chromatography in combination with mass spectrometry. "Hard base" refers to the anti-M Bismuth Journal of American Chemical

Society, 1 9635 85 "H / C" means the value determined by the original ASTM method D5291. Anion as described in P. 3533. The weight ratio of daughter hydrogen to atomic carbon. H / C is "heteroatom" as measured by the weight percent of carbon and carbon, and refers to the oxygen, nitrogen and / or contained in the molecular structure of the hydrocarbon; As determined by ASTM method E385 for oxygen, D5762 for nitrogen, and D 4 2 9 4 for sulfur. "Chlorine source" means tritium and / or a kind of reaction that reacts in the presence of crude oil feed and catalyst, and ki and hydrogen feed crude oil. Compounds and / or compound groups of one or more compounds. Hydrogen sources can include, but are not limited to, hydrocarbons (e.g., q to G hydrocarbons, such as methane, ethane, propane, butane, pentane, light oil), water, or mixtures thereof. Mass balance is used to assess the net amount of hydrogen supplied to one or more compounds in the crude feed.

Inorganic salt '' refers to a compound composed of a metal cation and an anion. “IP” refers to the Institute of Petroleum, and the current Central State is the Energy Institute of London, United Kingdom. O “Isoparaffin” refers to branched saturated hydrocarbons.

"Kerosene" means hydrocarbons with a boiling range between 204 and 260 ° C (400-500 ° C) at 0.101 MPa. The kerosene content is determined by ASTM method D2887. 41 200533738 Lewis "Acid" means a compound or substance having the ability to accept one or more electrons from another compound. Louis test means a compound and / or substance capable of giving one or more electrons to another compound. Cigarette smoke refers to hydrocarbons with carbon numbers ranging from 1 to 6. "Liquid mixture" means a composition containing one or more compounds that are liquid at standard temperature and pressure (25 ° C, 0.101 Mpa, hereinafter referred to as "STp"), or one or more compounds that are A composition in which a liquid compound is combined with one or more compounds that are solid under STP. "Micro-carbon residue, (" MCR ") refers to the amount of carbon residue remaining after evaporation and pyrolysis of the substance. The MCR content is as measured by ASTM method D453〇." Light oil "means at 0 · 101 The hydrocarbon content in the boiling range at MPa is distributed between U 0c and 204 C (100-400 0F). The content of light oil is determined by method D2887.

"Ni / V / Fe" means nickel, vanadium, iron, or a combination thereof.

Ni / V / Fe inclusion '' refers to the content of Ni / V / Fe in a matrix. The Nl / WFe content is as measured by ASTM method D5863.

Nm / m refers to standard cubic meters of gas per cubic meter of crude oil feed. "Non-acidic" refers to the properties of Lewis base and / or Bronister-Louis. "Non-condensable gas, refers to the standard temperature and pressure (25H10.1Mpa, hereinafter referred to as" STP ") as The composition and / or composition of the gas. "N-paraffins, which refer to normal (straight-chain) saturated hydrocarbons. The calorific value is the value of the internal combustion engine fuel compared with the standard reference fuel. 42 200533738 The value for calculating the anti-knock property is determined by D6730. Calculation of light oil The alkane number is such as the branched and straight, olefinic type of the olefin by the ASTM method. It refers to chemical additions with non-aromatic carbon-carbon double bonds, including, but not limited to, quaternary, trans, terminal, molecular, and chain. "Periodic Table" means the periodic table stipulated by the International Union of Pure and Applied Chemistry (IUPAC) in November 2003. Xifang compounds refer to compounds containing two or more aromatic rings. Examples of Xifang compounds include, but are not limited to, indene, naphthalene, anthracene, phenanthrene, benzothiophene, and dibenzothiophene. Residue refers to a component whose boiling range is distributed at 538 ° C (1000 F) or higher at 0.11 Mpa, as measured by ASTM method D5307. `` Semi-liquid '' refers to a material phase that has the properties of liquid and solid phases of the substance. Examples of semi-liquid inorganic salt catalysts include slurries and / or phases having a consistency such as toffee, pudding, or toothpaste. "SCFB" refers to the standard cubic foot of gas per barrel of crude oil feed. "Superbase" refers to substances that can deprotonate hydrocarbons such as paraffins and olefins under reaction conditions. " "TAN" means the total number of acids in grams of KOH ("mg,") per gram ("g") of the sample. TAN is as measured by ASTM method D664. "TAP" means transient analysis of the product. TMS refers to transition metal sulfides.

"VGO" refers to a component whose boiling range is distributed between 343 ° C and 53.8 ° C (65 (MO)) at 0 · 101 MPa. The vg〇 content is determined by ASTM 43 200533738 method D2887 In the context of this application, it is to be understood that if the value obtained for the :: = property falls within the limit of the test method: the test method is newly calibrated to test the property. It should be understood that Use other standardized test methods that are considered to be equivalent to 蒋, τ, J, k, and k and test methods 0 y

Crude oil can be produced from 3 fe products and / or viewed, and then made. Crude oil is usually solid, semi-solid and / or liquid. Crude oil may contain crude oil. Stabilization may include, but is not limited to, removing non-condensing compounds, water, salt, or a combination thereof from the crude oil to form a stable crude oil. This stabilization can be performed at or near the manufacturing and / or distillation site. Ingredients with an anorexia number of 4 or more are included in an amount of at least grams of ingredients per gram of crude oil. Examples of stabilized crude oils include whole crude oil, topped crude oil, and stabilized crude oil that has not generally been distilled and / or shredded in processing facilities to produce multiple components with a particular Foten range distribution (such as light oil, = Outflow 'VGO and / or lubricant). Distillation includes, but is not limited to, atmospheric distillation and / or vacuum distillation. Undistilled and / or unfractionated stable crude oil may

Desalted crude oil, desalted crude oil, or a combination thereof. "Topping, refers to a crude oil that has been processed so that at least some of its components with a boiling point below 35 at 0.101 MPa have been removed. Typically, topping crudes are at most 0.1 grams and at most 0.05 per gram of topping crude. Grams or up to 002 grams of such ingredients. Some stable crude oils have properties that allow stable crude oils to be transported to traditional processing facilities by means of transportation (such as pipelines, trucks or ships). Other 44 200533738 crude oils have a One or more of the inappropriateness that makes them inferior 胄. Inferior crude oil may be unacceptable to the means of transport and / or processing facilities, and therefore gives the inferior crude oil a very low economic value. The economic value may consist in accommodating what is considered A reservoir of inferior crude oil that is too burdensome in making &amp; transporting and / or handling.

The properties of inferior crude oil may include, but are not limited to: a) a UN of at least W; b) a viscosity of at least 0.2 Pa.s; c) a specific gravity of at most 19; d) 0.00005 grams less per gram of crude oil or at least 0 · 0001 Gram Ni / V / Fe total Ni / v / f &lt;

Content, e) total heteroatom content of at least 0.005 grams of heteroatoms per gram of crude oil; f residue content of at least 0.01 grams of residue per gram of crude oil; g) asphaltene content of at least 0 grams of asphaltene per gram of crude oil; h) MCR content of at least 0.02 grams of mcr per gram of crude oil; or a combination thereof. In some specific examples, the inferior crude oil series may include at least 0.2 g of residue, at least 0.3 g of residue, at least 0.5 g of residue, or at least 0.9 g of residue per gram of inferior crude oil. In some specific examples, the low grade crude oil contains 0.2 to 0.99 grams, 0.3 to 0.9 grams, or 0.4 to 0.7 grams of residue per gram of low grade crude oil. In certain specific examples, the low grade crude oil may have a sulfur content of at least 0.001 grams, at least 0.05 grams, at least 0.001 grams, or at least 0.02 grams per gram of low grade crude oil. Inferior crude oil may comprise a mixture of hydrocarbons having a range of boiling points. Inferior crude oil may include: at least 0.001 g, at least 0.005 g, or at least 0.01 g of a boiling range distributed between 2000c and 300 at 0.101 MPa. Hydrocarbons; at least 0.001 g, at least 0.05 g, or at least 0.001 g. Hydrocarbons having a boiling range between 0.001 c and 4,000 c at 0.001 MPa. ; And at least 0.001 g, at least 0.005 g, or at least 0.0005 45,033,738 g of hydrocarbons having a boiling range distributed between 400 0C and 700 0c at 0.101 MPa, or a combination thereof. In some specific examples, in addition to the higher boiling components, the low-grade crude oil may include at least 0.0001 grams, at least 0.05 grams, or at least 0.01 grams per gram of low-grade crude oil. Oi Mpa hydrocarbons with a boiling range distribution of up to 200 ° C. Typically, the inferior crude oil has a hydrocarbon content of at most 0.2 g or at most 0.1 g per gram of inferior crude oil. In some specific examples, the low grade crude oil may contain up to 0.9 grams or up to 0.99 grams of hydrocarbons with a boiling range distribution of at least 300 ° C per gram of low grade crude oil. In some specific examples, the low-grade crude oil may also contain at least 0.001 grams of boiling range distribution of at least 650 per gram of low-grade crude oil. (: Hydrocarbons. In some specific examples, inferior crude oil can contain up to 0.9 grams per gram of inferior crude oil or up to 0.99 grams of hydrocarbons with boiling ranges between 300 ° C and 1000 ° C. Available Examples of inferior crude oils processed by the methods described in this article include, but are not limited to, crude oils paid to the following countries and regions: Canada Alberta, Venezuelail Orinoco, Venezuela, Us s. So California Californian and north slope Alaska, Mexico Bay of Campeche, Argentina San Jorge basin, Santos and Kan, Brazil The Persian Basin (Brazilian Santos and Campos basins), China

Bohai Gulf, China Karamay, Iraq Zagros, Kazakhstan 46 200533738

Caspian), Nigerian Offshore (Nlgena〇ffsh〇re), the British North Sea (U) llted Kingd⑽ N ° rth Sea, Madagascar Northwest (Madagascar northwest), Oman [Ormn, "From Park a and 1 Uman" and Horam Humbek (Netherlands

Schoonebek) 〇 The treatment of inferior crude oil can increase the meaning of the shield and 丄 ^. The nature of advanced grade crude oil makes it acceptable for transportation and / or premises. The crude oil and / or inferior crude oil to be processed may be referred to as a "crude feed". The emu oil feed can be topped as planned. Using the methods described herein, crude oil products obtained from calendar, soil, and processing are suitable for transportation and / or refining. Continuing the original ^ Θ crude oil product's properties are closer to the counterpart of West Texas Intermediate (West T +, est Texas Intermediate) crude oil than the crude oil feed, or more right than the crude oil feed. (Brent) Corresponding secondary quality of crude oil therefore has an economic value of 4 shells compared with the economic value of the crude oil feed. The transport crude oil product can be refined with less or no pretreatment, thus improving the refining efficiency. The former virtual search I 4 service has removed impurities from crude oil products including desulfurization, demetallization, and / or atmospheric distillation. ... a method for contacting a crude oil feed according to the present invention is explained here. In addition, there are various specific concentrations of light oil, kerosene, diesel oil, and: specific examples of products, and they usually cannot be produced by traditional types of methods. Crude oil feeds can come from one or more contacts with chlorine. Contact in the presence of a medium in the contact area and / or in a combination of two or more contact areas. In the example, the wind source was generated on the spot. On-site generation of a hydrogen source may include reacting at least ___ Aba ^ 4 knife crude oil feed with an inorganic salt catalyst at a temperature ranging from c or 300-400 ° c to form hydrogen and / or light 47 200533738 Hydrocarbons. The on-site generation of hydrogen may include at least a portion of a reaction comprising an inorganic salt catalyst such as an alkali metal formate. The whole product usually contains gases, vapors, liquids or mixtures produced during the contact. The complete product contains crude oil products that are liquid mixtures under STp, and, in some specific examples, contains hydrocarbons that are non-condensable under STp. In some specific examples, complete products and / or crude oil products may include solids (e.g., inorganic solids and / or coke). In some specific examples, solids may be entrained in the liquid and / or vapor produced during contact. The contact zone usually includes a reactor, a part of the reactor, multiple parts of the reactor or multiple reactors. Examples of reactors that can be used to contact a crude oil feed with a hydrogen source in the presence of a catalyst include: stacked bed reactors, fixed bed reactors' continuous stirred tank reactors (CSTR), spray reactors, live base flow reactors, And liquid / liquid contactors. Examples of CSTR include fluidized bed reactors and ebullated bed reactors. Contact conditions typically include temperature, pressure, crude oil feed flow, complete product flow, residence time, hydrogen source flow, or a combination thereof. Contact conditions can be controlled to produce crude products with specific properties. The contact temperature range can be 200-800 ° C, 300-700 ° C, or 400-600 ° C ° In a specific example in which the hydrogen source is supplied as a gas (such as hydrogen, pinane, or ethane), the gas feeds crude oil. The ratio of material is usually in the range of UM 〇〇

Nm3 / m3, 2-8000 Nm3 / m3, 3-4000 Nm3 / m3 or 5-300 Nm3 / m3. Contacting is usually carried out in a pressure range between 0.1-20 Mpa, 1-16 Mpa, 2-10 Mpa, or 4-8 MPa. In some specific examples in which steam is added, the ratio of Zhongluo to crude oil feed is in the range of 0.01 kg, 0.03-2.5 kg, or 0.00 kg steam per kg of crude oil feed. The flow rates of raw, A, and A may be sufficient to maintain at least 10%, at least 50%, or at least 90% of the feed volume of the crude oil in the contact zone. The volume of crude oil in the total contact zone of the code zone is 40%, 60% and 60% of the total volume of the contact zone. In some specific examples, the 'contacting may be performed under an additional gas such as argon, or 80 alkane, propane, butane, propylene, butylene, or a combination thereof. Old Existence — Figure 1 Schematic diagram of a specific example of a contact system 100 used to make a complete product of vapor. Crude oil feed leaves crude oil supply source = in contact zone W. Amount of catalyst used in the contact zone = for contact £ 1GG grams of crude oil feed! _ Grams, 2_8G grams, 3_7Q grams or 60 grams of heart. In some specific examples, a diluent may be added to the feed to reduce the crude oil feed size. In some specific examples, the raw material enters the bottom of the contact · 102 via the conduit 104. In some specific examples, the crude oil feed may be before and / or during the feeding of the contact zone 102: the raw: the feed is heated to at least 100. . Or at least 300. . temperature. The standard 5 ′ can heat the crude feed to between 2% and 2%. ^ Temperature in range. In some specific examples', the catalyst is combined with the crude oil feed and then passed to the contact zone 102. The crude feed / catalyst mixture can be heated to at least 100 ° C or at least 300 before being fed into the contact zone 102. . temperature. In terms of type, the crude oil feed can be heated to a fine temperature of 50000c or 300-400 ° C. In some specific examples, the crude oil feed / catalyst mixture 49 200533738 is sludge. Pulp. In this specific case, &gt; and ‘specific examples, the crude oil feed may be before: the crude oil feed is fed into the contact Dian Anke ’s Ding An to reduce. Outstanding £ 200-300 〇c r m A at ι00_4〇〇. Adding 埶 々 e at the temperature in the L target garden or m can be added to the crude oil feed. When the crude oil is processed into the catalyst / catalyst mixture, the formation of the acidic constituents in T10 can be changed from 屌 ,, It is a salt of A. It is the TAN of some alkali metal rhenium. ^ Remove some acidic components from the raw material to reduce the original upper zone 1: In some cases, 'the crude oil feed is continuously added to the contact material / catalyst mixture. Mixing can be sufficient to inhibit the catalyst and crude oil from being removed at least ^ eight swords. In the examples, the catalyst can be regenerated from the contact area 102 and i. In some specific examples, this type of door is used. In some specific examples, fresh catalyst can be added to the contact zone 102 during the reaction program period. In some specific examples, the crude oil feed and / or the mixture of crude oil feed and inorganic salt catalyst is sent as an emulsion. Into the contact zone. The emulsion can be prepared by combining an inorganic salt catalyst / water mixture with a crude oil feed / surfactant mixture. In some specific examples, a stabilizer is added to the emulsion. The emulsion can be maintained Stable for at least 2 days, at least 4 days, or at least 7 days. Stable for 30, 10, 5 or 3 days. Interface / tongue agents include but are not limited to: organic polycarboxylic acids (Tenax 2 (^ 0; MeadWestvaco Specialty Product Group; Charleston, South Carolina, USA), C21 dicarboxylic fatty acid (DIACID 1550;

MeadWestvaco Specialty Product Group), petroleum sulfonate (Hostapur SAS 30; Clarient Corporation, Charlotte, North Carolina, U.S.A.), Tergital NP-40 surfactant (Union 50 200533738

Carbide; Danbury, Connecticut, U.S.A.) or mixtures thereof. Stabilizers include, but are not limited to, diethylene glycol (Aldrich Chemical Co .; Milwaukee, Wisconsin, U.S.A.) and / or monoethanolamine (j.

Baker; Phillipsburg, New Jersey, U.S.A.). The circulation catheter 106 may connect the catheter 108 and the catheter 104. In some specific examples, the 'circulation catheter 106 can directly enter and / or leave the contact area} 02. The circulation conduit 106 may include a flow control valve 110. The flow control valve 110 may allow at least a portion of the material to be circulated from the conduit 108 to the conduit 104 and / or the contact area 102. In some specific examples, the condensation unit can be placed in the duct 108 to allow at least a portion of the material to be condensed and recycled to the contact zone 102. In some specific embodiments, the circulation duct 106 can be a gas circulation Pipeline. The flow control valves 110 and: Π0 can be used to control the flow in and out of the contact area 102, so that a fixed volume of liquid is maintained in the contact area. In some embodiments &apos; a substantially selected volume range of liquid may be maintained in the contact zone 102. The feed volume in the contact zone 102 can be monitored using standard equipment. The gas inlet 1 1 2 can be used to add a hydrogen source and / or additional gas to the crude oil feed when the crude oil feed enters the contact zone 102. In some specific examples, the Lu 'fly inlet 114 can be used to add radon to the contact area 102. In some specific examples, the water-containing steam will get you into the contact zone 102 from Y, &gt;…, fly you, and work from the inlet 114. ... In some specific examples, at least-part of the complete product is produced as a vapor: contact zone 102. In some embodiments, the complete product is produced as steamed milk and / or as a vapor containing small amounts of liquids and solids from the top of the pad 102. The vapor was transported to the separation zone through a conduit, and the change was made. 51 200533738 The ratio of hydrogen source to crude oil feed in the contact zone 102 was 3 to v 0.5 g, at least 0 8 g, and at least 0-97 g of crude oil product. . The amount of steam produced in this area is two per gram; in two consecutive cycles: 0, 10 grams of crude oil are produced from the contact zone. It is believed that the catalyst and / or solids of the Jinkebao-gram or &quot;-sequence can be left in the contact area as a contact with Cheng Tian. The solid and / or used catalyst can contain residual crude oil feed and / Or coke. + In separation it 116, the vapor is cooled and separated using standard separation techniques to form crude oil products and gases. The crude product leaves the separation unit and enters the crude product receiver 119 via conduit 118. The resulting crude oil product I is suitable for transportation and / or processing. The crude oil product receiving H 119 may include a line, line, one or more storage units, one or more transportation containers or daggers, and in some specific examples, the separated gas (such as hydrogen Thorium oxide, carbon dioxide, hydrogen sulfide, or oxane) is transported to other Canadian dollars (for example, for use in fuel cells or sulfur recovery equipment) and / or recycled to the contact zone 102 via '100. In some specific cases, physical knife-off methods (such as filtration, centrifugation, or membrane separation) may be used to remove solids and / or liquids that are lost in the crude product. Fig. 2 Qitian depicts a contact system 122 for processing a crude feed with one or more catalysts to produce a finished product. The complete product may be a liquid or a liquid mixed with a gas or a solid. Crude oil feed may enter contact zone 102 52 200533738 via conduit 104. In some specific examples, the crude feed is received from a crude feed supply. The conduit 104 may include a gas inlet 112. In some specific examples, the gas inlet 112 may directly enter the contact area 102. In some specific examples, the steam inlet 114 can be used to add steam to the contact zone 02. The crude feed can be contacted with the catalyst in the contact zone 102 to make the complete product. In some specific examples, the catheter 06 allows at least a portion of the complete product to circulate to the contact zone 102. The mixture containing the complete product and / or solid and / or unreacted crude feed leaves the contact zone 102 and enters the separation via a conduit 108 = 124. In some specific examples, a condensing unit may be placed (e.g., in the guide 106) so that at least a portion of the mixture in the conduit can be condensed and cycled to the contact area for further processing. In some specific examples, Dun Chen '笞 106 can be a gas circulation line. In some specific examples, the guide 108 may include a filter to remove particles from the complete product. In the separation zone 124. At least a portion of the crude oil product can be produced from

(糸 is separated from the complete product. In some specific examples, the complete product and / or solid is recycled to the catheter body. It is circulated through the catheter to the contact: used catalyst and / or coke. The gas system of the P-knife is separated from the complete product

For further processing. Crude products can be derived by derivation. In some specific examples, crude oil products can be transported to a crude oil product receiver. In some specific examples, the complete product and / or crude oil product may include catalysts to the hydrazone portion. Gases entrained in the complete product and / or crude product can be separated using standard gas / liquid separation techniques such as spraying, membrane separation, and depressurization. In some specific examples &apos;, the separated gas is transported to other Guardian & (e.g., for use in fuel cells, sulfur recovery equipment, other processing units or combinations thereof) and / or recycled to the contact zone. In some specific examples, separation of at least a portion of the crude feed is performed before the crude feed is fed into the skin. Figure 3 is a schematic diagram of a specific example of a combination of a separation zone and a contact system. The contact system 13 () may be the contact system 100 and / or the contact system 122 (shown in FIGS. 1 and 2). The crude oil feed enters the separation zone 132 via the guide 104. At Thirty-two centimeters, standard separation techniques are used to separate at least a portion of the crude feed to produce separate crude feeds and hydrocarbons. The separated crude oil feed, in some specific examples, includes a mixture of components having a Foten range distribution of at least 100 oc, at least 120 oc, or, in some specific examples, includes a boiling range distribution of at least C. A typical and § "separated crude oil feed contains a mixture of constituents with a totem range between _ · _0 π, 12 ο γ, or ·.%. The hydrocarbons separated from the crude oil feed leave the separation zone 132 via a conduit 134 It is transported to other processing units, processing facilities, storage facilities, or a combination thereof. At least a portion of the separated crude oil feed leaves the separation zone 132 and enters the contact system 13 ′ via a conduit &quot; 6 for further processing to form a crude product. It leaves the contact system i 3 0 via the conduit 138. 54 200533738 In some specific examples, the shishi seven feed system f Μ $ any one of the methods described herein from crude oil into the crude oil product I, is a toilet. ^ ^ ^ /, A crude oil blended with the same or different crude oil feed. For example, the eight I, Yachu "a total of two crude oil gates with a high viscosity: the viscosity is between the viscosity of the crude oil product and the Crude oil "product. The resulting blended product can be suitable for transportation and / or processing. Figure 4 is a specific example of the combination of the first and first combinations of wo fish pull bar and contact system in the blending zone. In some specific examples, The main crude oil product exits the contact system via the channel 138, and σ ^^ 40. 40. In the blending zone, a portion of the crude oil product and-or multiple processing streams (such as 4 hydrocarbon streams or light oil from multiple crude oil feeds), crude oil, crude oil feeds, or mixtures of them to make blended products. Processing streams, crude oil, crude oil, or mixtures are sent directly to the blending zone 14 ( ) Or via 'Lu 142¾ to the upstream of the blending zone. The mixing system can be located in or near the pushing zone Mo. The blended product can meet specific product specifications. Specific product specifications-unlimited table. A range or limit of API Specific gravity, TAN, viscosity, or a combination of daggers. The blended product is transported and / or processed by leaving the blending zone 14 through f 144. In some specific examples, methanol is used as a catalyst during the contacting procedure. 丨For example, lice and monoxide can react to form methanol. The recovered methanol can have ridged salts such as potassium hydroxide. The recovered methanol can be combined with additional crude oil feed to form a crude oil feed / methanol mixture. Feeding methanol with crude oil And it is easy to reduce the viscosity of the crude oil feed. Heating the crude oil feed / methanol mixture to at most 500 cC can reduce the ταν of the crude oil feed to less than 1. 55 200533738 Figure 5 shows the combination and blending of the separation zone and the contact system. Schematic illustration of a specific example of a combination zone. The crude oil feed enters the separation zone 132 via the conduit 104. The crude oil feed is separated as described previously to form a separate crude feed. The separated crude feed enters contact via the conduit 1 3 6 System 130. The crude product leaves the contact system 130 and enters the blending zone 140 via the conduit 1 38. In the blending zone 140, other processing streams and / or crude oil sent via the conduit 42 are associated with the crude product. Combine to form a blended product. The blended product exits the blended region 140 via a conduit 144.

FIG. 6 is a schematic diagram of a multi-contact system 146. The contact system 100 (shown in FIG. 1) may be placed before the contact system 1 48. In an alternative embodiment, the positions of the contact systems may be interchanged. The contact system includes a salt catalyst. The contact system 148 may include one or more catalysts. The catalyst in the contact system 148 may be an additional inorganic salt catalyst, a transition metal sulfide catalyst, a commercially available catalyst, or a mixture thereof. The crude oil feed enters the contact system 100 'via a conduit 104 and is then contacted with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product A 70 The entire product contains hydrogen and, in some specific examples, a crude oil product. The complete product can exit the contact system 100 via a catheter 108. Hydrogen generated from contacting the inorganic salt catalyst with the crude feed can be used as a hydrogen source for the contact system 148. At least part of the hydrogen system generated is

The contact system 100 is transmitted to the contact system 148. In an alternative embodiment, the hydrogen produced and / or separated may be separated and then transferred to the contact system 148 via the conduit 150. In some embodiments, the contact system 148 may be part of the contact system 100 such that the generated hydrogen flows directly from the contact system 100 to the contact system 148. In 56 200533738 these specific examples, the vapour stream produced by the contact gas 1GG is directly mixed with the crude oil feed into the contact system 148. The second crude oil feed is via the conduit 52 into the contact system] 48 in the contact system 148; 、, 占, 仓 t t is obtained by contacting the crude oil feed with at least a portion of the gas catalyst produced— Species of product. Fei and dhai products are complete kings in some specific examples. The product is exiting the contact system 148 via the conduit 154. In some specific examples, a system including a contact system, a contact zone, and / or a blending zone, such as those shown in the figure, may be located at or near a manufacturing site that manufactures inferior crude oil feeds. After processing through the catalyst system, the crude feed can be considered suitable for transportation and / or use in a refining process. In some specific examples, crude oil products and / or blended products are shipped to refining and / or processing facilities. Crude products and / or blended products can be processed to make commercially available products, such as transportation fuels, heating fuels, lubricants, or chemicals. Processing may include steaming and / or branching crude oil products and / or blended products to make one or more branches. In some specific examples, crude oil products, blended products, and / or one or more fractions may be hydrotreated. In some specific examples, the complete product is at most 0.05 grams, at most 0.03 grams, or at most 0.01 grams of coke per gram of complete product. In some presenting examples, the complete product is substantially free of coke (i.e., coke is not detectable). In some specific examples, the crude oil product is per gram of crude oil product: coke containing at most 0.05 g, at most 0.03 g, at most 001 g, at most 005 g, or at most 0. g. In certain specific examples +, the crude oil product has a range from 0 or more to 0.05, 0.000001_003 grams, 0.000001-0,01 grams, or 0.001-0.005 grams per gram of crude product. Coke content, or 57 200533738 is undetectable. In certain specific examples, the crude product has an MCR content of up to 90%, up to 80%, up to 50%, up to 30%, or up to 10% of the Mcr content of the crude feed. In some specific examples, the crude product has a negligible MCR content. In some specific examples, the crude oil product is an MCR of at most 0.05 g, at most 3.0 g, at most 0.01 g, or at most 0.001 g per gram of crude product. Typically, crude oil products contain MCR from 0 g to 0.04 g, 0.0001 to 03 g, or 0.0001 g to 1 g of crude oil product. φ In some specific examples, the complete product contains a non-condensable gas. Non-condensable gases typically include, but are not limited to, carbon dioxide, ammonia, hydrogen sulfide, hydrogen, sulphur oxide, methane, other hydrocarbons that are not condensable under STP, or mixtures thereof. In some specific examples, hydrogen, carbon dioxide, carbon monoxide, or a combination thereof can be formed as a% by contacting steam and light hydrocarbons with an inorganic salt catalyst. Typically, under thermodynamic conditions, the molar ratio of carbon monoxide to carbon dioxide is 0-7. In some specific examples, the molar ratio of the carbon monoxide produced to the carbon dioxide produced is at least 0.3, at least 0.5, or at least 0.7. In some specific examples, the molar ratio of the carbon monoxide produced to the dioxide produced is in the range of 0.3 to 10, 0.4 to 0.9, or 0.5 to 0.8. The ability to generate carbon monoxide over carbon dioxide on the spot can benefit other processes located near or upstream of the process. For example, the carbon monoxide produced can be used as a reducing agent in the treatment of hydrocarbon formations, or in other processes such as syngas processes. 58 200533738 In some specific examples, the complete product u as prepared herein contains a boiling dry enclosure + Ί Λ n J packages C and 538. (: The compound mixture between the side mixture can be made of Lu Shijin. Hydrocarbons in the range of 4 to 4. The mixture is a mother Keating species mixture 玎 5 J ^ material contains 0.001_0 8 grams, 0.003 0.005-0 . (^ Grams of € _ ^ brother u · 1 grams or 4 workers ,. c4 hydrocarbons per gram of c4 hydrocarbons can be 0.001-0.8 grams per gram, 〇0 (η π) 4 cheek Γ contains .1 grams Or 0.005-0.01 grams of butadiene. Right- /, in the case of 'iso-chain hydrocarbons, up to 1 $, up to 4, up to 1, 0, up to 0.8 , At most 0.3 or at most 0.1

Than made. In this example, the isoparaffin system is based on a hard pit of 0.00001-1 with respect to normal hydrocarbons, 0, 0 〇Λ, or 0 · 0001-1 · 0 or 0 · 001- A paraffin having a weight ratio in the range of 0.1 may include an isoparaffin and / or a normal paraffin.

In some specific examples, the complete product and / or crude oil product may include olefins and / or paraffins in proportions or miles that are not normally found in crude oil T produced from the product and retorted. The olefin contains a mixture of an olefin (, olefin) having a terminal double bond and an olefin having an intramolecular double bond. In some specific examples, the olefin content of the crude oil product is 2, 10 greater than the olefin content of the crude oil feed. , 50, 100, or at least 200. In some specific examples, the olefin content of the crude product is a factor of up to 1,000, up to 500, up to 300, or up to 250 compared to the olefin content of the crude feed. In some specific examples, hydrocarbons with a boiling range in the range of 200-400c have hydrocarbons with a boiling range of 20-400 CC in the range of 0.001-0.1 g, 0.0001-0.05 per gram Grams or olefins in the range of 0.01 to 0.44 grams. In some specific examples, at least ㈦ grams, at least 0.005 grams, or at least, 0.01 grams of alpha thin smoke can be produced per gram of crude oil product. In some specific examples, 59 200533738, the 'crude oil product contains 0.0001_05 grams, 0.00 1-0.2 grams, or 00 Hi grams of alpha olefin per gram of crude oil product. In some specific examples, Hydrocarbons with a boiling range of 20-400 have a boiling range of 20- Hydrocarbons between 400 have an alpha dilute hydrocarbon content in the range of 0.0000 g, 0.0001 g, or 0.01-0.04 g. In some specific examples, the boiling range is distributed at 20 -204. (: Hydrocarbons between: at least 0.7, at least 0.8, at least 009, at least 10, at least

The weight ratio of olefins to intramolecular double-bonded olefins is 1.4 or at least 1.5. In some specific examples, hydrocarbons with boiling ranges between 20-204 ° C have a weight ratio of olefins to molecular p double bonds olefins in the range of 0 ^ 10, 0.8-5, 0.9-3, or 1β2 . The α-olefin pair of crude oil and city f product is intramolecular, and the weight ratio of bonded olefins is at most 0.5, which is at most 0.5. This ability to produce alpha sulfonium, which has an increased amount of olefins with intramolecular double olefins, and alpha tellurium in κ ', can help turn crude oil products into commercially available products. In some specific examples, the crude oil feed and the chlorine source are contacted with an inorganic salt catalyst at the lower θ to produce a boiling range containing linear dilute hydrocarbons distributed in n.

0 C hydrocarbons. The straight-chain dilute hydrocarbon has cis and trans double bonds. Reverse: Double-bonded linear olefin pairs and cis ★ The weight ratio of straight-chain olefins with double bonds is to 0.4, to 10 or ^. In some specific examples, a straight-chain dilute hydrocarbon pair with a trans ^ bond and a cis + 'T 丨 丨 shell-type double bond linear olefin 0.001-1.4' 〇01 1 n -¾ η, 圯 疋 〆H .0 or 0 丄 0.4. In some specific examples, Futten yoke is distributed in the f range of 20-204 0C, and the right Beigu 1 cheek has a boiling range of 20 grams to 400 grams.

The hydrocarbons within the range are at least 0 to 0.2 L, and the main paraffin content is 0.1 g, at least 0.15 g, at least 0 20 g, or 0.30 g. The normal paraffin content of such hydrocarbons may be in the range of 0.001 to 0.9 g, 0.1 to 0.8 g, or 0.2 to 0.5 g per gram of hydrocarbons. In some specific examples, such hydrocarbons have a weight ratio of isoparaffins to normal paraffins of at most 15, at most 14, at most 1.0, at most 0.8, or at most 0-3. From the normal paraffin content of such hydrocarbons, it can be estimated that the normal paraffin content of crude oil products is in the range of 0.001 to 0. 9 grams, 0.001 to 0.8 grams, or 0.01 0.5 grams per gram of crude oil products. Inside. In some specific examples, the crude product has a total Ni / V / Fe content of 90%, up to 50%, up to 10%, up to 5%, or up to 3% for the crude feed. . In some specific examples, the crude product is a mother gram crude product that contains at most 0 0001 grams, at most i X 5 grams, and at most 1 X 10-6 grams of Ni / V / Fe. In certain specific examples, the crude oil product has between 1 x 10-7 grams to 5 x 10-5 grams per gram of crude product, 3 x 7 grams to 2 X 100.5 grams or i x 10-6 grams to i Total Ni / v / Fe content in the range of χ 10- 5 grams. In some specific examples, the crude product has a TAN that is at most 90%, at most 50%, or at most 10% of the TAN of the crude feed. In some specific examples, the crude product may have a TAN of at most i, at most 0.5, at most 0 m, or at most 0.05. In some specific examples, the ταν of the crude product may be in the range of 0.001 to 0.5, 0.001 to 02, or 0.05 to 0.001. In certain embodiments, the API specific gravity of the crude product is at least 10%, at least 50%, or at least 90% higher than the API specific gravity of the crude feed. In some specific examples, the Aρ specific gravity of the crude oil product is between 13_50, 15_ such as or 16-20. 61 200533738 In some specific examples, the content of the child is at most 70% and at most. In some specific examples, the content is at least 10%, at least the amount. The crude oil product has a total heteroatom of 50% or up to 30% of the total heteroatom of the crude oil feed. The crude oil product has a total heteroatom of 40% or at least 60% of the total heteroatom of the crude oil feed. The sulfur content of the feed is up to 90%, up to 70%, or up to 6G%. The sulfur content of crude oil products, based on per gram of crude oil product, may be at most 0.02 g, at most 0.0 g, at most 0.05 g, at most 4 g, and at most _3. G or at most 0 · _g. In certain embodiments, the &apos; crude oil product has a sulfur content in the range of 0.0001-2.00 g or 0.005-0.01 g per gram of crude product. In some specific examples, the crude oil product may have a nitrogen content of the crude oil feed = 90% or more or 80% or less. The nitrogen content of the crude oil product may be at most 41, at most 3 g, or at most 0.0 G1 g per gram of crude product. In some specific examples, the crude oil product has a nitrogen content in the range of 0.00000 -1 005 fragrant Br or 0.0001 gram per gram of crude oil product. In some specific examples, the crude oil product contains 0.05-0.2 grams or 0.09-0.15 grams of hydrogen per gram of crude product. The h / c of the crude product may be at most 1.8, at most 1.7, at most U, at most 5 or at most 14. In some specific examples, the H / C of the crude product is 80-1250% or 90 110/6 of the crude feed 11/0 :. In other specific examples, the crude product is 100-120% of the crude feed H / C. The crude oil product H / C within 20% of the crude feed H / c indicates that the absorption and / or consumption of hydrogen in this process is minimal 62 200533738. Crude products contain ingredients with a range of boiling points. In some specific examples, the crude product contains: at least 0.001 grams or from 0.0001 to 0.5 grams with a boiling range distribution of up to 200 at 0.101 MPa. (: Hydrocarbons up to 204 ° C; at least 0.001 g or from 0.001 to 0.5 g of hydrocarbons with a boiling range between 200 ° C and 300 ° C at 0.101 MPa; at least 0.001 g or from 0.001 to 0.5 g of hydrocarbons with a boiling range between 300 ° C and 40 ° C at 0.101 MPa; and at least 0.001 g or from 0.001 to 0.5 g of boiling ranges between 400 0C and 53 8 0C at 0.101 MPa In some specific examples, the crude oil product has a light oil content of 0.00000-0.2 g, 0.0000-0.00 g, or 0.001-0.05 g per gram of crude oil product. In some specific examples, the crude product contains 0.001-0.2 g or 0.005 g of light oil. In some specific examples, the light oil contains at most 0.15 g per gram of light oil, Up to 0.1 g or up to 0.05 g of diene. In some specific examples, the 'crude oil product line contains 0.005 g / g, 0.5 g / g of crude oil product. 0.1 grams or 0.0001-0 olefins. In some specific examples, Xin light oil has at most 0.01 grams, at most 0.05 grams, or at most 0.5 grams per gram of light oil. Benzene content of 2 grams. In some specific examples, light oil has an undetectable or between 1 x 10.7 grams to 1 X 1 0-2 grams, 1 x 10-6 grams to 1 X 10.5 Benzene content in the range of gram, j χ 104 gram to 1 X 10-4 gram. The composition containing benzene can be regarded as a hazard in processing, so crude oil products with relatively low benzene content may not require special treatment. In some specific examples, the light oil may contain aromatic compounds. Aromatization 63 200533738 Compounds may include monocyclic compounds and / or polycyclic compounds% Compounds may include, but are not limited to: benzene, toluene, o-xylene , M-xylbenzene, p-dimethylbenzyl, ethylbenzyl, ethyl ethyl 3 -fluorenylbenzene; κethyl · 2-methyl: methyl ,, 3 -methylbenzyl 'trimethylbenzyl; Phenylbenzene

2-propylbenzene; 2-ethyl ", 'difluorenylbenzene; 2-ethyl_2,4 · dimethylbenzene · i'2'3,4-tetramethylbenzene; ethyl, Amylfluorenylbenzene; u: ethyl tetramethylfbenzene; triisopropyl, xylene; substituted homologues of benzene, xylene, o-xylene, m-xylene, p-xylene or mixtures thereof. Monocyclic弋 # compounds are used in a variety of commercially available products and / or crude oil products prepared as described herein with H = ° alone typically have an increased aromatics content.

In some specific examples, the crude oil product has a methylbenzyl content of 0.001-0.2 g, 0.05-0.15 g, or 0.011 g per gram of crude oil product. The raw product product has a m-xylene content of 0.00 bg, 50000 g, or 0.05-0.08 g per gram of crude oil product. The crude oil product has an o-xylene content of = 0.0001-0_2 grams, o.oos-o "grams, or 0.0001 grams per gram of crude oil products. The crude product has a p-xylene content of 0.0000 g, 0.005 to 0.08 g, or 0.0006 g per gram of crude product. An increase in the content of aromatic compounds in a light oil tends to increase the octane number of the light oil. Crude oil can be evaluated based on an estimate of the crude's gasoline potential. Gasoline potential can include, but is not limited to, the octane number calculated for the light oil portion of crude oil. Crude oils usually have a calculated octane number in the range of 35-60. The octane number of gasoline tends to reduce the need for additives that increase the octane number of gasoline. In certain specific examples, the crude product comprises a light weight having a calender value of at least 60, at least 70, at least ⑽ 64 200533738, or at least 90. Typically, the octane number of light oil is in the range of 60-99, 70-98, or 80-95. In some specific examples, &amp; φ, compared to the total light oil and kerosene content in the crude oil feed, the square compound content,

No &lt; ΛΛ Jing, the products in the boiling range of 204 ° C and 500 ° C hydrocarbons (She She Yun # 仏 人 ~ light oil and kerosene,) have a higher ~, square compound Content, and higher than 0 /, ^. To 5%, at least 10%, at least 50% or at least 99%. Kang type and 'to &amp; &amp; person eight °' The total content of total light oil and kerosene in the crude oil product without compound content is higher than the total aromaticization of total light oil and kerosene in crude oil into the "" set 8% higher , 20%, 75% or 100%. In some specific examples, snail oil and light oil may have a total polyaromatic compound content in the range of 0.0001.0.5 grams, 0.0001-02 grams, or 100,000 grams per gram of total kerosene and light oil. The crude oil product has per gram of crude oil product which has a gallium content in the range of 0.0001-0.9 g, 0.01-0.5 g, 0.005-0.3 g, or 0.001-0.2 g. In some specific examples, the weight ratio of kerosene to diesel in the remaining effluent is in the range of 1.4 to 1 ^ 2.5 to 5: 2. In some specific examples, the crude oil product contains at least 0.001 g per gram of crude oil product, from 0 to 0.7 g,

Brother υ · ϋ〇1-〇 · 5 grams or 〇 01_0J grams of kerosene. In certain embodiments, the crude product contains 0.001-0.5 g or 0.01-0.3 g of kerosene. In the case of the diffusive substance, the kerosene has at least 0.2 grams, at least 0.3 grams, or at least 0.4 grams of aromatic compounds per gram of kerosene. In some specific In the examples, the kerosene has an aromatic compound content per gram of kerosene in the range of 5 grams or from 0.2 to 0.4 grams. In some specific examples, the freezing point of kerosene may be _30. 匚 or less, _ 65 200533738 40 〇 Below C or Qiao 〇〇c υ π _ From below. The increase in the bitter content of the kerosene portion of the crude oil product tends to combine the low freezing point with the known method. The density of the kerosene portion of the crude product can be added and refined. To produce crude oil-producing fuels with = density and low freezing point. # ^^, degree and money_ nature of aviation thirsty wheels. Two V :: 'Crude oil products are per gram of crude oil products with at 0.1 grams, at least U grams of oil is per square gram of the square compound content. In some specific examples, chai ^ square compound in the range of ο · 1.1 grams, G.3 · 0.8 grams or grams Content. In some specific examples, the crude oil product is produced per gram of crude oil. With • 1-0.99 g, from 0.001-0.8 g, or from 〇i 3 η VG〇5 See the specific range of θ from 0.1 to 0.3 g. In some specific examples, the VGO content in crude oil products: and: ΐ Crude oil products in the range of 0.4 · 0.9g or 0.6-0.8g. In a certain column, the VGO system has 〇1_〇99g, 〇3_ or 0 per gram of VG. Aromatic compound content in the range of 5 to 0.6 grams. In the two specific examples, the crude oil product has at most 50%, at most 30%, at most 10%, or at most 1% of the crude oil feed. Residual = Γ ° In some specific examples, the crude oil product has at most //.1 g, at most 0.05 g, at most 0.03 g, at most 0.02 g, at most 2. Residual content of 0.005 grams or up to 0.001 grams. _ = In specific examples, crude oil yields ^ 0.1 grams, 0.0001-0.05 grams, 0.001-0.03 grams or 0.005- 66 200533738 0.04 grams of residue content. In a specific example, the crude oil product may include at least part of the specific examples. In a specific example, the crude oil product contains a large, gram but less than 0.01 g, 〇._〇〇1_〇 per gram of crude oil product. 〇1g or 〇〇_ncuck catalyst. The catalyst can help the army during Θ / bucket, during transportation and / or processing in processing facilities: 疋 crude oil products. The catalyst can inhibit corrosion and friction And, or increase the water separation capacity of crude oil: Crude oil products containing at least a portion of the catalyst can be processed in one step to make lubricants and / or other commercially available products.

"The catalyst used to process the crude oil feed in the presence of a hydrogen source to produce a complete product" is: an earlier catalyst or multiple catalysts. The catalyst used in this application may first be a catalyst: a 'fouling agent' which is in hydrogen and / or containing The sulfur crude oil feed is converted into a catalyst in the contact zone when it comes into contact with the catalyst precursor. Sealing the catalyst used to contact the crude oil feed with a hydrogen source to make a complete product can help reduce the molecular weight of the crude oil feed. No To be bound by theory, the combination of catalyst and gas source can reduce the amount of radon in crude oil feed through the role of alkaline components (Lewis base or Brewster _).

in. May have a Lewis base and / or a Bronister-Rore base. Examples include the catalysts described herein. In some specific examples, the catalyst is a TMS catalyst. The TMS catalyst contains a compound containing a transition metal sulfide. For this application, the weight of the transition metal sulfide in the TMS catalyst is determined by adding the total weight of the transition metal to the total weight of sulfur in the catalyst. The transition metal-to-sulfur atomic ratio is usually in the range of 0 to 20, 0.5 to 10, or 5%. Examples of transition metal sulfides can be found in "Inorganic Sulfur 67 200533738" edited by G. Nickless; &quot; Inorganic Sulfur chemistry &quot;; Elsevier Publishing

Company; Amsterdam — London-New York; Copyright 1968) Chapter 19. In some specific examples, the TMS catalyst system may include one or more transition metal sulfides per gram of catalyst in total of at least 0.4 g, at least 0-5 g, at least 0.8 g, or at least 0.99 g. In some specific examples, the TMs catalyst system has one or more transitions per gram of catalyst in the range of 0.4-0.0999 grams, 0.5-0.9 grams, or 0.6.0.8 grams. Total metal sulfide content.

TMS catalysts contain one or more transition metal sulfides. Examples of transition metal sulfides include: pyrite (Fe45Ni45S8), pyrite (Fe6_75Ni2.25Sn), galena (1 ^ 7 Qin. ^ 〇.] 32), tetragonal ore (FyNi) ^ s ") 'Yinlu pyrite (Α§ι ^ ΝίΛ), isometric Cuban ore (CuFe2S3), isometric chalcopyrite, amphibole (Zno.95Feo.05S), limonite, sulphur Tin-Iron Complex (CU6FeSn2S8) 'Pyrite (), Chalcopyrite (), I1 Member Pyrite (FeS), Pyrite (F s)

-, T eb2) magnetite (Fe (1_x) S (x = 〇 to 0-17)) 'Hematite Γ 1st; q, + taxi, N (3S2) or galena ( NiS2). In some specific examples, the TMQ 丄 一 人 MS T TMS catalyst contains one or more transition metal stone waste compounds in combination with alkali metals, soil test metals, zinc, Syrian, Chinese, or annual compounds, or mixtures thereof. In this case, the case is described in the following example. The TMS catalyst is represented by the general chemical formula A c [MS &amp;]. Alkaline earth metal or zinc; w represents a transition metal selected from columns 6-10 of the Periodic Table of the General, Dian, and Luos; and S is sulfur. The atomic ratio of α is in the range of 0.5 to 1.5, γ λ 1 to 5 or 1 to 2. (The atomic ratio to α is 0.0001 to], πΛ. B is in the range of 0.1 to 0.8 or 0.3 to 0.5. 68 200533738 In some specific examples, the transition metal is iron. In some specific examples, the TMS catalyst May contain commonly known metal test and / or alkaline earth metal / transition metal sulfides (such as limonite (K3FeIGSI4), pyrite (K3FeIGSI4), pyrite (K6NaFei9Cu4NlS26C1), chlofenite Ore (K61Fe24Cu.2S26 / 1. 7) and / or ferrierite (NaFe3S5. (H2〇) 2). In some specific examples, the 'TMS catalyst contains limonite ore prepared on the spot. The limonite potassium ore can be referred to as artificial limonite potassium ore. Natural and / or artificial limonite unloading can be used as a TMS catalyst in the methods described herein. In some specific examples, the TMS catalyst system Each 100 grams of TMS catalyst can contain 3 to 25 grams, up to 15 grams, or 1 gram of carrier material. Code 3L. TMS catalyst contains 0 to 25 grams per 100 grams of TMS catalyst.

0001 to 20 g, 10,000 to 10 g of carrier material. Examples of carrier materials that can be used with milk media include refractory oxides, porous carbon materials / vernite or mixtures thereof. In some specific examples, the TMS catalyst is consistently free or free of carrier material.逦 II TMS catalysts for alkali metals, zinc, zinc compounds, or mixtures thereof may contain one or more transition metal sulfides, bimetal alkali metal-transition metal sulfides, high-valent transition metal sulfides, transition metal oxides Or a combination thereof, as measured using diffraction. Part of the metal, earth, metal, and / or transition metal sulfide composition of the tms catalyst 'In some specific examples, it is an amorphous composition that cannot be detected by X-ray diffraction technology presence. 69 200533738 In some specific examples, the grains of the TMS catalyst and / or the mixture of TMS catalyst grains have a particle size of at most 108 A, at most 103 A, at most loo A, or at most 40 A. In general practice, the particle size of the TMS catalyst grains is usually at least 10 A. TMS angle media containing alkali metals, alkaline earth metals, zinc, zinc compounds, or mixtures thereof can be obtained by mixing a sufficient amount of deionized water, a required amount of a transition metal oxide, and a required amount of a second metal carbonate , 1-2th metal oxalate, 1-2th metal acetate, carbonate, zinc acetate, zinc oxalate or a mixture thereof to prepare a wet paste. This wet paste can be made at i. . -3〇. Dry at 150-250 ° C to form a transition metal oxide / salt mixture. The transition metal oxide / salt mixture can be in the range of 300-1000C, 500-800. (: Or 600-700 γ calcination to form a transition metal oxide metal salt mixture. The transition metal oxide metal salt mixture can react with hydrogen to form a reduced intermediate solid. The addition of hydrogen may be sufficient to provide an excess Hydrogen to the transition metal oxide metal salt mixture at a flow rate. Hydrogen can be added to the transition metal oxide metal salt mixture over a period of 10-50 hours or 20-40 hours to produce a reductant containing elemental transition metal. Intermediate solids. Hydrogen addition can be performed at a temperature of 35-500, 50_4 () 0. (: 戍 1000 300 and Η5 MPa ,; Π-14 MPa or i2_13 Mpa. It should be understood that The reduction time, reaction temperature, choice of reducing gas, pressure of reducing gas, and / or flow rate of reducing gas to prepare the intermediate solid are usually changed relative to the absolute mass of the selected transition metal oxide. In some specific examples 'The reduced intermediate solids can pass through a 40-mesh screen with minimal force. 70 200533738 The reduced intermediate solids can be increased with controlled heat release and gas generation rates. Add to a hot (eg 100% diluent / elemental sulfur and / or sulfur- or compound mixture). The diluent may include any suitable diluent that provides a means of dispersing the heat of vulcanization. The diluent may include a boiling range of eight At least E, at least 15., less than 200, or at least: two solvents. Usually the diluent has a Teng Fan Shibu between 100_500 oc, 150_400 oc or Shenggang V. In some cases, The diluent is VG0 and / or xylene. Sulfur compounds include, but are not limited to: hydrogenated hydrogen and / or thiols. The amount of sulfur and / or sulfur compounds is ranked first among metal salts or salts!- The number of moles of 2 metal or rhetoric is used as a reference, and the range can be from W00 mole%, so-called mole%, 5-5g mole% u mole

%. After adding the reduced intermediate solids to the diluent / elemental sulfur mixture, 'the resulting mixture may be heated incrementally to a final temperature of 2000-500cc, 2500-4500Y, or 00-4GG, And maintained at this final temperature for at least ^ jt to 2 hours or at least 10 hours. Typically, the final temperature is maintained for 15 hours, 1 G hour, 5 hours, or 1.5 hours. After application to the elevated vulcanization reaction temperature, the diluent / catalyst mixture can be cooled to between C 30-90. (: Or 50-80. (: Temperature in the range to help recover the delta catalyst from the mixture. Using standard techniques, the sulfurized catalyst can be removed from the diluent in an oxygen-free atmosphere; I: catty Is, Mining and extraction: ,,, and then washing at least a part of a low boiling point solvent (such as pentamidine, heptane or hexane) to prepare a TMS catalyst. The TMS catalyst can be powdered using standard techniques. In two specific examples, the catalyst is an inorganic salt catalyst. The anions of the inorganic salt catalyst include inorganic compounds, organic compounds, or mixtures thereof. Inorganic 71 200533738 Salt catalysts include metal carbonate, metal hydroxide, Metal hydride, metal amine, metal sulfide, metal acetate, metal oxalate, metal phosphonate, metal pyruvate, metal carbonate, metal hydroxide , Soil metal hydride, soil metal amine, soil metal sulfide, soil metal acetate, soil metal oxalate, alkaline earth metal formate, alkaline earth metal pyruvate or mixtures thereof. Vehicles include, but are not limited to, a mix of : NaOH / RbOH / CsOH; KOH / RbOH / CsOH; NaOH / KOH / RbOH; NaOH / KOH / CsOH; K2C03 / Rb2C03 / Cs2C03; Na20 / K20 / K2C03; NaHC03 / KHC03 / Rb2CC3; Li / R032K03 K2C03 / Rb2C03 / Cs2C03 KOH / RbOH / CsOH mixed; K2C03 / CaC03; K2C03 / MgC03; Cs2C03 / CaC03; Cs2C03 / Ca0; Na2C03 / Ca (0H) 2; KH / GsC03; KOCHO / CaOO CsOCHO / Ca (OCHO) 2; NaNH2 / K2C03 / Rb20; K2C03 / CaC03 / Rb2C03; K2C03 / CaC03 / Cs2C03; K2C03 / MgC03 / Rb2C03; K2C03 / MgC03 / Cs2C03; or mixed with K2CCC / C2C03 OH) 2. In some specific examples, the inorganic salt catalyst contains at most 0.00001 grams, at most 0.001 grams, or at most 0.01 grams of lithium per gram of inorganic salt catalyst, which is calculated based on the weight of lithium. In some specific examples, inorganic Salt catalysts contain lithium per gram of inorganic salt catalyst from 0 g but less than 0.01 g, 0.0000001-0.001 g, or 0.00001-0.0001 g, based on the weight of lithium. In some specific examples, the inorganic salt catalyst contains One or more metallurgical salts containing an alkali metal of at least Π in the original 200533738 subsequence. + In some specific examples, when the inorganic salt catalyst contains two or more pieces of alkali gold M, the working ratio is%, and the atomic ratio of an alkali metal having an atomic number less than 11 to an alkali metal having an atomic number greater than 11 is 0. · 1 to 10, 0 · 2 to 6 or 0.3 to 4 in the range of 0. For example, inorganic salt catalysts can include sodium, potassium, and osmium salts, where the ratio of sodium to potassium is In the range of 0.1-6; the ratio of sodium to ytterbium is in the range of 0.1 to 6; meat, and the ratio of unpaired gal is in the range of 0.1 to 1-6. In another embodiment 1J, the inorganic salt catalyst comprises a sodium salt and a potassium salt, wherein the atomic ratio of sodium to potassium is in the range of 0.1 to 4 in the county. In some specific examples, the inorganic salt catalyst also includes a metal selected from the eighth to the tenth table of the periodic table, a compound selected from the eighth table to the metal, a metal selected from the sixth table of the periodic table, Compounds or mixtures of metals on the sixth table of the periodic table. The metal package selected from columns 8-10 includes, but is not limited to, iron, nails, inscriptions or notes. Metals selected from column 6 include, but are not limited to: chromium, pins or cranes. In some specific examples, the inorganic salt catalyst contains 0.1-0.5 g or 0.2-0.4 g of Raney nickel per gram of the inorganic salt catalyst. In some specific examples, the inorganic salt catalyst also includes a metal oxide selected from columns 1-2 and / or 13 襕 of the periodic table. Metals selected from ^^ include but are not limited to: delete or inscription. Non-limiting examples of metal oxides include oxidized bell (u2〇), oxidized oxide (K2〇), oxidized feed (c aluminum oxide (αι2〇3)). 4 Ru Haihai inorganic salt catalyst in some specific examples Does not contain or is substantially non-obstetric acid ⑷a Bcl3, Alcl) S03), cloth tau Luo ^ 歹 1 σ H3〇, h2S〇4, HC1 and HN〇3), gas-forming composition such as salt and salt Evening salt) and halide. Inorganic salt catalysts per gram of inorganic salt catalyst 73 200533738 may contain: from 0 g to 0 g, 0.0000 g 0.001 g, or 0.00001 to 0.005 g. A) halide; b) at least 35,000 MC or a gas-forming composition at a temperature of up to 1000 ° C; c) Luxianbenchong, w) yeast acid, d) Bronister-Roreic acid; or e) a mixture thereof . Inorganic salt catalysts can be cracked using standard techniques. For example, quasi-mixing techniques (such as grinding and / or crushing) can be used to combine the required amounts of catalyst into individual knives. In other concrete examples, φ., Is to dissolve the inorganic composition in a solvent such as water or a suitable organic solvent) to form an inorganic composition / solvent mixture, which can be removed by the technique of ionization, to obtain an inorganic salt catalyst. . # 中 ^ 例 巾 ’Push inorganic catalyst salt without catalyst into the carrier to form an inorganic salt catalyst on the carrier. Examples of the carrier include, but are not limited to, agricultural lice, calcium oxide, oxidized town, &quot; lice titanium, hydrotalcite, alumina, emulsified germanium, iron oxide, nickel oxide, oxygen, θ human lice zinc, lice Cadmium, antimony oxide, and their products. In some concrete cases, φφ can immerse the inorganic salt, the metals in columns 6-10, and ‘or the 6-1 棚 genus into the compound of the genus immersion in the carrier. Alternatively, the inorganic salt catalyst can be formed by melting, or softening the inorganic salt with ,,, or impregnated in and / or on the can, or monsoon carrier or metal emulsion carrier. Touch: When a certain structure is at a preset temperature or a temperature range where a sequence of 4 degrees of loss occurs in the catalyst structure, the recitation of the halls, air seconds, etc. will become uneven, permeable, and / or relocatable. The inorganic salt catalyst can change (for example, there is no decomposition of the salt ^ there is no substantial change in the formation m ^ ^ ^ It is not bound by theory, when the distance between the salt salt catalyst and the salt ion of the inorganic salt catalyst increases Become None ...: As the ion distance increases, the crude oil feed and / or hydrogen source can penetrate through the inorganic salt catalyst, rather than across the surface of the inorganic salt catalyst. Crude oil feed 74 200533738 Feed and / or hydrogen source penetrates through the inorganic salt Often, the contact area between the inorganic salt catalyst and the crude oil feed and / or hydrogen source is increased. The increase in the contact area and / or the active area of the inorganic salt catalyst can generally increase the yield of crude oil products and limit residues> Investigate and / or produce coke and / or promote changes in properties of crude oil products compared to the same properties of crude oil feed. Disorders of inorganic salt catalysts (such as non-uniformity, permeability and / or migration) can be used DSC Method, ion conductivity measurement method, TAP method, visual inspection, X-ray diffraction method, or a combination thereof. The method for measuring catalyst characteristics using TAP is described in the following U.S. Patent Nos. Issued to Ebuer 4,626 for others , 412; 5,03,489 to Gleaves et al .; and 5,264,183 to Ebner et al. TAP systems are available from Mithra Technologies (Foley, Missouri, US A.). TAP analysis is available at 25-85. 〇 、 5〇_5〇〇〇c or 60.4。 00, in the temperature range of 10_50〇c or .20_40〇c heating rate and: 1 X 10 13 to 1 X 1〇- Performed under vacuum in the range of 8 Torr. The temperature can be maintained constant and / or increased as a function of time. As the temperature of the inorganic salt catalyst increases, the gas emitted by the inorganic salt catalyst is measured. Examples of gases include-carbon oxide, carbon dioxide, 1, water, or a mixture thereof. A turning point (a sharp increase) in the release of an inorganic salt catalyst gas is detected @ temperature is considered to be the temperature at which the inorganic salt catalyst becomes disordered. .J In some specific examples, the turning point of the exhaust gas of the inorganic salt catalyst may be within a range of temperatures, such as those measured using TAp. This temperature or = temperature range is called "TAP temperature". The temperature range measured using TAp The starting temperature is called the "minimum TAP temperature." Exhaust gas exhibited by inorganic salt catalysts contacted by crude oil feed: ㈣ is within ___, Gang_5⑻. C or dove · copper. C is within the τΑρ temperature range. Typically, the ΤΑρ temperature is within 30.5 〇〇… Scope—In the case of limbs, different compositions of suitable inorganic salt catalysts also show gas turning points' but at different TAP temperatures. The size of the ionizing turning points related to the exhaust gas can be in the crystal structure Particle-human order index. In a highly ordered crystal structure, ionic particles are usually tightly associated, so ions, molecules, gases, or combinations thereof require more energy to release from the structure = (that is, more Of heat). In the disordered body, the ions are not strongly associated with each other like the ions of the highly ordered crystal structure. Due to the association of this lower ion, release from the disordered crystal structure, ions, molecules and / or gases usually require less energy, and therefore, at the degree of selectivity, the disordered crystal structure is released. The ion and / or gas = k is greater than the "ift" of the ion and / or gas released by the ordered crystal structure of the same degree. In a general example, when differential scanning calorimetry is used, The heating rate or cooling rate can be measured from 5G to ·. The dissociation heat of the inorganic salt catalyst was observed in the range c. In the DSC method, the sample can be heated to the first temperature, cooled to room temperature ', and then heated again. The transitions observed during the first underheating usually represent the entrained water and / or solvent, but this does not represent the heat of dissociation. For example, it is easy to observe that the dry heat of my hydrated samples can usually appear at 250. . The following, blood type:, between purchase M). Observed during the cooling cycle and the second heating: The transition to is equivalent to the heat of dissociation of the sample. "Cold" thermal transition "means that ordered molecules and / or atoms in the structure become free during DSC analysis

"Transformation" refers to the process that occurs when ordered molecules and / or atoms in a structure become more uniform during a temperature analysis when the temperature decreases. In some specific examples, the heat / cold of inorganic salt catalysts The transition occurs within the dry enclosure / dish degree measured using dsc. The temperature or temperature range where the inorganic salt catalyst thermal transition occurs during the second heating cycle is called "Dsc temperature". The temperature during the second heating cycle The lowest DSC temperature of the range is called "max + dsc temperature,". Inorganic salt catalysts are available at 200-5. c, 25 (M5 () Qc or _400% range exhibits a thermal transition.… In inorganic salts containing inorganic salt particles in a fairly homogeneous mixture, 2 varies with the temperature during the second heating cycle. The peak of the heat absorption may be quite narrow. The inorganic salt containing inorganic salt particles in a rather heterogeneous mixture may be contacted with the #, as it is during the second heating cycle. The peak of the heat may be broad. I DSC spectrum towel Scanned temperature of online shirt catalogue

-No heat is absorbed or released within the consumption range. No thermal transition usually indicates that the sample structure does not change when heated. The homogeneity of particles in the inorganic salt mixture increases, and the ability of the mixture to maintain solid and / or semi-liquid during the period decreases. Inorganic mixing uniformity may be related to the ionic radius of the cations in the mixture. For a cation having a radius of 2 to 2, the cation is together with the corresponding anion; the ability of the electron pull is increased ', so the acidity of the corresponding anion is increased. As for the column of similarly charged ions, 'If the anion is a hard base, the ionic radius of the shell' results in a higher ion between the cation and the anion. Tends to result in a salt with a higher thermal transition temperature and / or a more caustic, homogeneous particle mixture in the salt (sharper spikes and increased areas below the DSC curve,,,, and area). This mouthpiece of cations tends to be more acidic than cations with large ionic radius, so: the acidity of organic salt mixtures increases with decreasing cation radius. For example, crude oil feed and hydrogen source in the presence of an inorganic mixture containing bell cations Contact 'compared to the original; from the contact of the feed with a hydrogen source in the presence of an inorganic salt catalyst containing cations with a larger ion radius than lithium, tend to produce increased amounts of gas and / or coke. Gas suppression And / or the capacity of coke production increases the total liquid product yield of the sequence.

In some specific examples, the inorganic salt catalyst may include two or more ware-less minimum DSC temperatures for each of the inorganic salts. The minimum DSC temperature of the inorganic salt catalyst may be below the minimum DSC temperature of at least one of the inorganic metal salts in the inorganic salt catalyst. For example, the inorganic salt catalyst may include potassium carbonate and cesium carbonate. Potassium carbonate and carbonate shavings exhibited a DSC / dish greater than 500. The K2C03 / Rb2C03 / Cs2C03 catalyst exhibits a DSC temperature in the range of 290-300 ° C. In some specific examples, the TAP temperature may be between the DSC temperature of at least one of the inorganic salts and the DSC temperature of the inorganic salt catalyst. For example, the TAP temperature of inorganic salt catalysts can be in the range of 350-500 ° C. The D S C temperature of the same inorganic salt catalyst can be between 2 0-3 0 0. In the range of C, the DSC temperature of individual salts can be at least 500 ° C or at most 1000. In many specific examples, I machine pedals that have a TAP and / or DSC temperature between 150-500 ° C, 200_450 or 300-400 0C and do not decompose at these 78 200533738 temperatures ... It can be used to catalyze the conversion of high molecular weight and / or viscosity components (such as horse oil, crude oil feed) to liquid products. In some specific examples φ, + ^ Behr, at 200-600 ° C, 300-500. (: Or 350-450 ℃ temperature chart ^ q ^ &amp; During the internal heating of inorganic salt catalysts, inorganic salt catalysts can show an increase compared to individual touches * _ ^ ', ..., 1 Electrical conductivity. The increased conductivity of inorganic salt catalysts is usually caused by the particles in the inorganic salt catalysts becoming transferable.-The temperature at which the ionic conductivity of some inorganic salt catalysts changes is higher than that of the inorganic salt catalysts. Middle position _ V., ν Warm production with change in ion conductivity

low. Also determined by Ohm's law: J /: = Μ, the ionic conductivity of the inorganic salt can be applied. The eighth κ 疋 pressure / / is the current, and Λ is the resistance. To measure ionic conductivity ', an inorganic salt catalyst can be placed in a quartz container provided with two metals, wires (such as copper wires or platinum wires) separated from each other but immersed in the inorganic salt catalyst.

Figure 7 is a schematic diagram of a system that can be used to measure ion conductivity. The Shiyang Valley 156 containing the sample port 158 may be placed in a heating device and gradually heated to a desired temperature. A voltage from the power source 16 was applied during heating: the metal wire I62. The resulting current passes through the metal wires 162 and 164 and is measured at the meter 166. Meter 166 M (but not limited to) a multimeter or Wheatstone bridge. As sample 158 becomes more non-uniform (more mobile) without decomposition, the resistance of the sample should decrease and the current observed in the meter should increase. In two specific examples, the inorganic salt catalyst may have different ionic conductivity after heating, cooling, and then heating at a desired temperature. The difference in ionic conductivity can indicate that the crystal structure of the inorganic salt catalyst has been changed from the original shape (the first shape energy) and the eighth, to the different shape during the heating period (after the second centroid heating, If the inorganic salt catalyst is not changed during the heating period, the ionic conductivity is expected to be similar or the same. '... In some specific properties, the inorganic catalyst has a range of 0 ... 100 micron range. The measured grain salt catalyst of 2 meters is passed through a net or sieve. The 5 Hai Wutian inorganic salt catalyst is heated to 5G γ or more and 5 ⑼. C or less: Degree k may month b H When the inorganic salt catalyst is softened, the liquid and the catalyst particles can coexist in the inorganic salt catalyst matrix. In this case, in the case of the dimer, the catalyst particles are heated to a temperature of at least 300 ° C or at most _ Under gravity or under the dust force of at least 7Mpa or at most GMpa, it can self-deform, so that the inorganic salt catalyst changes from the first form to the second form g. When the salt catalyst is cooled to PC, the inorganic salt catalyst's No .: Form cannot be ㈣ = No.-form of organic salt catalyst. Inorganic salts from The transformation from one form to the second is called "deformation, temperature. The deformation temperature can be a temperature range or a single degree. In some specific examples, the inorganic salt catalyst particles are heated below any of the individual inorganic metal salts. When the deformation temperature is below the deformation temperature, it will deform itself under gravity or pressure. In some specific examples, the inorganic salt contains two or more inorganic salts with different deformation temperatures. In some specific examples, the 'inorganic salt' The deformation temperature of the catalyst is different from the deformation temperature of individual inorganic metal salts. In some specific examples, the inorganic salt catalyst is liquid and / or semi-liquid at or above the TAP and / or Dsc temperature. In some specific examples, The inorganic salt catalyst is liquid or semi-liquid at the minimum TAP and / or DSC temperature. At 80 200533738 minimum TAP and / or DSC temperature or above, In the two specific examples, the liquid or vehicle is mixed with the crude oil feed, Feeding materials ... The salt catalyst will form a phase separated from the crude oil. In some specific examples, at a minimum M temperature, a liquid or semi-liquid inorganic salt catalyst will feed crude oil per gram of raw material. The feed is from 0 g to 0.05 g (for example, 0.01 g, 0.00000 H2 g or g of inorganic salt catalyst) or crude oil insoluble (for example, per gram of oil The feed is from 0 g to 0.05 g, and the original gram of inorganic salt catalyst is 10,000 g.). 5 · 001 · 0 · 001 In some specific examples t, the powder H diffraction method is used to The interval of the atoms in the thermomechanical salt catalyst. The shape of the X-ray spectrum can be used to estimate the longevity of the 001 peak of the inorganic salt particles. The W and peaks in the human order χ-ray diffraction represent the inorganic salt. Different compounds of the catalyst. In the diffraction of γ and all η I tertiary χ-rays, D ". The peak can be used to estimate the interval between atoms. In inorganic salt catalysts containing inorganic salt atoms, the peak shape is relatively narrow. In: iCOs / Rb ^ / cv with (,,,,,,, or) inorganic salt atoms in a regular order (for example, broad, the shape of the D ten peaks may be equivalent to the D_ peaks may not exist. To measure the gate during the addition period e wood + w… machine | atomic disorder,… “can I change it?” can get the inorganic salt catalyst in X-ray diffraction pattern, and compare it with the material shot after heating. 〇〇c acquired temperature above /, Yao-shot corresponding to FIG dark do :( inorganic atom) may not exist, or than 5. :: achieved at a temperature in the X- ray diffraction pattern, a broad edge In 〇C with other inorganic salt @ x_ray diffraction pattern:, D001 peaks, showing a relatively narrow under the phase gate / dish degree 81 200533738 In addition to limiting and / or inhibiting the generation of by-products ^ ^ ^ 7 In addition, the contact strip can be controlled: the composition of the composition (that is, the product of the crude oil) can be predetermined: :: one: change. The complete product composition includes but is not limited to: paraffin, your warp, square compound or basin ,, This compound is followed by 4 ^ 7. These compounds constitute a composition of crude oil products and non-condensable hydrocarbon gas. Control The combination of catalytic conditions and the catalysts described in this article can produce complete products with lower coke yields than expected. Compare the roles of various crude oils ^ Yes: Crude oils can be classified according to their tendency to form coke. For example, with: per Crude oil (Mg MCR with MCR content of crude oil is expected to form more coke than crude oil with an MCR content of 0__g MCR per gram of crude oil. Inferior crude oil usually has an MCR content of at least GG5 mcr per gram of inferior crude oil In some specific examples, the residue and / or coke content deposited on the catalyst during the reaction may be at most 0.01 g, at most g, or at most 0.03 g of residue and / or coke per gram of catalyst. In some specific examples, the weight of the residue and / or coke deposited on the catalyst is in the range of 0.00000 g, 0.001-0.05 g, or 0.01-1-0.03 g. In some specific examples, the used catalyst is free of residues and / or coke. In some specific examples, the contact conditions are controlled so that there is at most 0.05 g per gram of crude oil product and at most 0.01 Of coke, at most 0.005 g or at most 0.003 g. The feed is in contact with the catalyst under controlled conditions, as opposed to heating the crude oil feed in the presence of refined catalyst or in the absence of catalyst by using the same contact conditions. Produces reduced coke and / or residual fishing. 82 200533738 In some specific examples, the contact conditions can be controlled such that there is at least 0.5 grams, at least 0.7 grams, at least 0.8 grams, or at least 0 grams per gram of crude oil feed. · 9 grams of crude oil feed is converted into crude oil products. Typically, between 0.5-0.99 grams, 0.6-0.9 grams, or 0.7-0.8 grams per gram of crude oil feed during contact Crude products are produced. The crude feed is converted to a crude product with minimal residue and / or coke production (if any) in the crude product, so that the crude product can be converted to a commercial product at a refinery with minimal pretreatment. In certain specific examples, at most 0.2 grams, at most 0.01 grams, at most 0.05 grams, at most 0.03 grams, or at most 0.01 grams of crude oil feed per gram of crude oil feed is converted to non-condensing Smoke. In some specific examples, 0 to 0.2 grams, 0.0001 to 0.1 grams, 0.0001 to 0.05 grams, or 0.00001 grams of non-condensable smoke are produced per gram of crude oil feed. Controlling the temperature of the contact zone, the flow rate of the crude oil feed, the flow rate of the complete product, the flow rate and / or amount of the catalyst feed, or a combination thereof, can be performed to maintain the desired reaction temperature. In some specific examples, the temperature in the contact zone can be terrible ... the flow of gaseous hydrogen sources and / or inert gases through the contact zone is performed to dilute the lice and / or remove excess heat from the contact zone. In some specific examples, the temperature in the contact zone can be controlled such that the temperature in the contact zone = temperature is the desired temperature, ν, or above or below. Some specific properties 'the difficult to touch temperature makes the contact zone', TAP temperature And / or the minimum temperature is below the minimum to the jump / dish degree. In some specific examples, the tau 2 ... AP temperature and / or the minimum temperature is below 30. Bu below 2: c or below 10. 0. For example, ' At a temperature of TAP and / or minimum field temperature, the temperature of the DSC can be adjusted to 3 ° C, 3 ° 0 ° C, or 3 ° 9 ° C during the reaction. In other specific examples, the contact temperature is controlled such that the temperature is or higher than the catalyst TAP temperature and / or the catalyst DSC temperature. For example, when a small TAP temperature and / or a minimum DSC temperature is 45 °, During the reaction, the contact temperature can be set to 450 ° C or 500 ° C or 5500 ° C. The contact temperature can be controlled according to the catalyst temperature and / or the DSC temperature of the catalyst to obtain improved crude product properties. For example, This control reduces coke formation: reduces non-condensable gas generation or their Combination.

In some specific examples, the phase-free salt catalyst can be adjusted before the crude oil feed is added. In some specific examples, this adjustment may be performed on the crude feed stock. Adjusting the inorganic salt catalyst may include heating the inorganic salt catalyst to at least ⑽ C, at least 300 ° C, at least 400 ° C., 25 I Γ ^ UC or at least 500. (: a first temperature, and then The medium is cooled to at most 250 ° C, at most 20 ° or 100. (: The second temperature. In a 4b and 1 /, system, the inorganic salt catalyst is heated to

The temperature is then cooled to 25-240. [, 30-200. … ―Fan! ::: Di Er temperature. The temperature can be adjusted by measuring the ratio of ionic two = to two two and the cooling inorganic salt at different temperatures. The adjustment of the catalyst can allow the temperature of the catalyst to be treated by adding chlorine to the crude oil feed. The reaction temperature in some specific examples of the content of the complete product, light oil, residual liquid, can be modified by changing the rate of removal of the complete product from contact with VGO or its mixture 84 200533738. And ^ ^, Niu 1 "said, reducing the rate of complete product removal, increasing the crude oil's ancestors 'total yang, and ^ drying the shell to the Jinke catalyst's contact time. Or =: =' can increase the contact Time, ^ is the mixture of the crude oil feed or hydrogen into the crude oil product at the flow rate, or the combination of the gate ^ when the contact of the bulk feed and the catalyst increases can be changed ° crude oil feed φ, , Ά, compared with wood oil, kerosene, light oil, and VG0 produced in a short contact time ... Pay ,, you, medium, and account for h ⑻ 而 &amp;, can increase the amount of Diesel kerosene or light oil and the reduced amount of vrn t ^ m ^ ^. Increasing the total product in the contact zone and contacting 4 can also change the crude oil time to obtain the ancient # dan1, * thousand average stone anorexia. Increased contact

proportion). Lower carbon number (and therefore higher API). In some specific examples, the contact conditions can change over time. For example, 1 can increase the contact force and / or contact temperature to increase the absorption of crude oil feed. 1. The change of hydrogen absorption of crude oil feed can improve other crude oil feeds on the same day, and increase the types of crude oil products that can be paid from a single crude oil feed. Outer II Π-, ^ 1 Manufacture of a variety of crude oil products from the early one crude oil feed: different transportation and / or processing specifications of Lico can be met. The absorption of chlorine can be compared by comparing the crude oil feed H / The production of C Shao crude oil products is estimated to increase the crude oil product H / C relative to the crude oil feed H / C. The increase indicates that chlorine is added to the crude oil product from a hydrogen source. The crude oil production AH / C is relatively low. (When compared with crude oil feed) indicates that there is a relatively low air consumption during processing. A significant improvement in the properties of the crude product obtained with minimal hydrogen consumption relative to the crude feedstock is desirable. The ratio of hydrogen source to crude oil feed can also be changed to change the properties of crude oil products. For example, adding a source of hydrogen to the crude feed oil product has a crude product that increases the VGO content. It is shown that the contact between the crude oil feed and the inorganic salt catalyst in the presence of light hydrocarbons in the presence of zeolite and the crude oil in the two examples is compared with the crude oil feed in the presence of the inorganic salt catalyst. The contact is because coke produced more liquid in the crude oil product. In specific examples that include the contact between crude oil feed and methylbenzene in an inorganic salt, the crude oil product has at least-part of the composition: the original cut and A (from A

Zhang Yuan). In one case, the volume of crude oil products produced by crude oil feeds in which the scriptures and hydrogen sources are contacted in the presence of inorganic salt catalysts is at least 5 times larger than the volume of crude oil products produced by thermal processes under STP. %, At most 彡 ⑽ or at least 1 or at most 100%. The total volume of the crude oil product produced by contacting the crude oil feed with the inorganic salt catalyst may be at least 110% by volume of the volume of the crude oil feed at STp. The increase in volume is believed to be due to the decrease in density

Caused by. The lower density is usually due, at least in part, to the hydrogenation of the crude feed. In certain specific examples, each gram of crude oil feed contains at least 0.02 grams, up to 0.05 grams, or at least 0.00 grams of sulfur, and / or at least 0.001 grams of Ni / v / Fe raw / source feed system. Contact with a hydrogen source in the presence of an inorganic salt catalyst without impairing the catalyst's activity. In some specific examples, the inorganic salt catalyst may be at least partially regenerated by removing one or more / defective components of the catalyst. Contaminants include, but are not limited to: metals, sulfides, nitrogen, coke, or mixtures thereof. Sulfide contaminants 86 200533738 can be removed from used inorganic salt catalysts by contacting steam and carbon dioxide with used catalysts to produce hydrogen sulfide. Nitrogen contamination can be removed by contacting the used inorganic salt catalyst with steam to produce ammonia. Coke contaminants can be removed from used inorganic salt catalysts by contacting the used inorganic salt catalyst with steam and / or formazan to generate hydrogen and carbon oxides. In some specific examples, one or more gas systems are produced from a mixture of an inorganic salt catalyst and a residual crude oil feed. In some specific examples, used inorganic salts (e.g., K2C03 / Rb2C03 / Cs2C03; K0H / Al2〇3; Cs2C (VCaC〇3;

KaOH / KOH / LiOH / ZrO2), unreacted crude feed and / or residue and / or coke mixtures are heated to 700-1000 or 800 in the presence of steam, hydrogen, carbon dioxide and / or light hydrocarbons A temperature in the range of -900 ° until the generation of gas and / or liquid is minimized to produce a liquid phase and / or a gas. The gas may include an increased amount of hydrogen and / or carbon dioxide relative to the reaction gas. For example, the gas may include from 01 to 99 moles or 0.2 to 8 moles of hydrogen and / or carbon dioxide per mole of reactive gas. The gas may contain relatively low amounts of light hydrocarbons and / or carbon monoxide. For example, less than 0.05 grams of light hydrocarbons per gram of gas and less than 0_01 grams of carbon monoxide per gram of gas. The liquid phase may contain water, for example, greater than 0.5-0.99 grams or greater than 0.9-0.9 grams of water per gram of liquid. In some specific examples, used catalysts and / or solids in the contact zone can be treated to recover metals (such as vanadium and / or nickel) from the used catalysts and / or solids. Used catalysts and / or solids can generally be treated using known metal separation techniques, such as heating, chemical treatment, and / or gasification. Examples 87 200533738 Non-limiting examples of catalyst preparation, catalyst testing, and systems with controlled contact conditions are described below. · Preparation of K-Fe sulfide catalyst. A K-Fe sulfide catalyst system is prepared as follows: 1000 g of iron oxide (Fe203) and 58 g of carbon fee _ are combined with 4 12 g of deionized water To form a wet paste. The wet paste was dried at 200 ° C to form an iron oxide / carbonic acid oblique mixture. The iron oxide / potassium carbonate mixture was calcined at 500 ° C to form an iron oxide / potassium carbonate mixture. This iron oxide / potassium carbonate mixture is reacted with hydrogen to form a reduced intermediate solid comprising an iron metal. The addition of hydrogen was performed at 4500C and 115] 2 2 Mpa (1665-1765 psi) for 48 hours. The intermediate solid was passed through a 40-mesh screen with minimal force. The intermediate solid is added incrementally at a controllable exothermic rate to generate a gas to the VGO / m-xylene / elemental sulfur mixture. After adding the middle door solids, the resulting mixture was gradually heated to 3 Torr. C and maintained at 300 ° C} hours. The solvent / catalyst mixture was cooled to 100 ° C. and the sulfurized catalyst was separated from the mixture. The sulfurized catalyst was isolated by transitional isolation in a dry box under an argon atmosphere, and then washed with @xylene to obtain a K Fe &amp; catalyst. The catalyst was pulverized by passing the sulfide catalyst through a 40-mesh screen. The obtained K_Fe sulfide catalyst was analyzed using X-ray diffraction technology. From the analysis of the X-ray diffraction pattern, it was determined that the catalyst contains sulfur-bearing iron, K Fe 4 compound (KFeS 2), pyrrhotite, and iron oxide (for example, magnetite 'Fe304). In this χ-ray diffraction pattern, no peaks related to iron and iron (such as pyrite and FeSj) were observed.

The sulfide catalyst was in contact with I 88 200533738. "A 600 ml continuous stirred tank reactor (consisting of 3 16 stainless steel) was equipped with a bottom inlet feed inlet, a single steam flow outlet, three thermocouples and shafts inside the reactor. Run a 125-inch six-blade Rushton turbine. A K-Fe sulfide catalyst (10.3 g) prepared as described in Example 1 was charged into the reactor. Hydrogen was metered into the reactor at 8,000 NmVin3 (50,000 SCFB) and mixed with asphalt (Lloydminster region, Canada). The bitumen enters the reaction state through the bottom inlet feed to form a hydrogen / crude oil feed mixture. During the 8-hour reaction operation period, hydrogen and crude oil feed were continuously fed into the reactor, and the product was continuously taken out through the reactor's outflow steam port. The crude feed was fed at a rate of 67.0 grams / hour to maintain the crude feed level at 60% of the reactor volume. The level of liquid in the reactor was measured using a 50 micro-Curie] 37Cs gamma-ray source and a sodium iodide scintillation detector. The hydrogen / crude feed was fed with catalyst at 430. (: Contact at the average internal reactor temperature. Contact of the hydrogen / crude oil feed with the catalyst produces a complete product in the form of the reactor effluent vapor. The reactor effluent vapor passes through the single upper lumen outlet to dilute the valley. The reaction is electrically heated at the top to 4 300 ° C to avoid condensation of the reaction effluent vapor inside the top of the reactor. After leaving the reactor, the reactor effluent vapor is cooled and cooled in a high pressure gas / liquid separator with low pressure gas / Separation in a liquid separator to produce a liquid stream and a gas stream. The gas stream is sent to a countercurrent alkaline scrubber to remove acidic gases, and then quantified using standard chromatography techniques. Complete product is 0918 grams of crude product per gram of complete product. And 0.089 grams of non-condensable hydrocarbon gas. In the reactor, there are 0.027 grams of solid residue per gram of 89 200533738. The properties and composition of the product and non-condensable hydrocarbon gas obtained by this method are summarized in the figure. : Table 2 and Figure 3 of the figure. Jin] Figure 9 This example demonstrates a method for making a crude oil feed in contact with hydrogen in the presence of a transition metal sulfide catalyst to produce a complete system with minimal coke pollutants. The complete product contains a liquid mixture under STp and gram of the complete product contains at most .1 gram of non-condensable flue gas. Separation by comparison Table 1 _ MCR content of crude oil feed (137 wt. The solids (27% by weight) formed during the method, the combination of visible / systematic conditions and catalysts produced a lower amount of coke than the two-space as shown by the as ™ method D4530. Non-condensable hydrocarbons include 0: 2, dagger And .4 hydrocarbons. From the sum of the weight percentages in Table 2 (20_5 grams), the ethylene content per gram of total c2 can be calculated. The c2 hydrocarbons of the flue gas contain 0. milk grams Ethylene. From the sum of the weight percentages of C3 hydrocarbons listed in Table 2, ⑺9g) '/ calculate the propylene content per gram of total hydrocarbons. Ck for non-condensable hydrocarbon gas: member cg total c3 hydrocarbons Contains 0.21 g of propylene. The non-condensable c-hydrocarbons have a weight ratio of isobutane to n-butane of 0.2. 4. This embodiment demonstrates a method for preparing a crude oil product including the following. At least Please 1 g boiling range distribution is at most 204 under GH) 1MPa. . (400 π) of hydrocarbons, at least 0.001 g distributed in the range of 0 μ μ. Smokes between c and 300 ° c, smokes with a boiling range of at least 0022 · 101 mp &amp; distributed between 300 ° C and 400 ° C and at least 0.001 grams. The boiling range is distributed at ··· at 101 MPa. . With 90 200533738

Hydrocarbons between 538 ° C_ (1,000 oF). Hydrocarbons distributed below 204 ° C contain isoparaffins and n-, ^ ^ ^ n-hydrocarbons at a ratio of at most ". And &quot; Iso-hydrocarbons for this crude oil product include with light oil, kerosene, diesel And boiling point distribution. The crude oil product contains P, P, D, and L々 ^ 0.001 grams of light oil, and the light oil portion of the crude oil product has ^ Γ oil portion with up to _ benzene benzene per gram of light oil Content. = The light oil portion of the product contains at most 0y ”pb% ΛΑ per gram of light oil. The fineness of the shoulder / product contains at least :, aromatic compounds per gram of light oil. · See The crude product contains at least 0.001 grams of kerosene and kerosene fractions having less than _30. The fraction of the crude product contains a suspected solidification point for aromatics. The kerosene portion of the crude product and the The kerosene portion of the crude oil product has an aromatic content of various ancient, gram square compounds. The kerosene portion of the shoulder square contains at least two compounds per gram of kerosene. Every day 7 early 3% clothes type aromatics The crude oil product contains at least diesel oil containing aromatic ... grams of diesel oil. The crude product has compounds per gram, and the "M" of the emu oil product and the crude product has at least _g: the VGO part contains aromatic "less than 0.5 grams of aromatics of the crude product" and the qing has See the known aromatic content of the compound. The solvent was released in a hydrocarbon to release the heterogeneous UC-Fe sulfide. The clothing was prepared as follows: 1000 g of iron oxide and 173 91 200533738 g of stone inverse acid were combined with 423 g of deionized water to form a wet paste. The wet paste was processed as described in Example 1 to form an intermediate solid. The intermediate solid was passed through a 40-mesh Xue Ge with minimal force. In contrast to the implementation of W 2, the intermediate solids and elemental sulfur are in the absence of hydrocarbon dilution J. 5 In a dry box using an argon atmosphere, the intermediate solids are mixed with powdered 7 L element sulfur and placed in a sealed carbon steel. In the tube, heat to C ° and hold at 400 c for i hours. The vulcanization catalyst is recovered as a solid from the carbon steel reactor. The potassium-iron sulfide catalyst was pulverized into a powder using a mortar and pestle so that the obtained catalyst powder could pass through a 40-mesh sieve. The X-ray diffraction technique is used to analyze the obtained potassium iron sulfide catalyst. From the analysis of the X-ray diffraction pattern, it was determined that the catalyst contains pyrite (), iron sulfide (Ues) and pyrrhotite (Fei xS). No mixed potassium-iron sulfide or iron oxide species were detected using the beam-wrapping technique. The polymerization, crude oil feeding, and reaction steps were the same as in Example 2, but the ratio of hydrogen to crude oil feeding was 16,000 Nm3 / m3 (1⑽, _ SCFB). A K-Fe sulfide catalyst (75.0 g) prepared as described in Example 3 was charged into the reactor. The properties of the crude oil products obtained by this method are summarized in Table 1 of FIG. 8 and Table 3 of FIG. 10. The weight percentage of VG0 produced in Example 4 is greater than the weight percentage of VG0 produced in Example 2. Knife ratio, Bewan also in Example 4 so that the weight percentage of the effluent obtained is less than the weight percentage of the effluent produced in the implementation. The weight ratio of the crude oil product prepared in Example 4 is lower than the specific gravity of J of the crude oil product prepared in Example 2. The higher 92 200533738 API specific gravity table does not produce hydrocarbons with higher carbon numbers. After contact with the crude feed, the TMS catalyst in the reactor was analyzed. From this analysis, we know that the transition metal sulfide catalyst contains K3Fe ^ S ^ after being in the presence of crude oil feed and hydrogen. In all TAP experiments, 300 mg samples were taken in a TAp system reactor at a rate of 500 c per minute from room temperature (27 c). Exhaust water radon gas and carbon dioxide gas system using this Ding Ap

System for mass spectrometer monitoring. Table contained in oxidation! The K2C〇3 / Rb2C〇3 / CS2C〇3 catalyst on Lu Shang showed that the carbon dioxide discharged from the inorganic salt catalyst has a current turning point greater than ο volts and the discharged water has G.G1 volts. Current turning point. Minimum: AP temperature is 3600 ° C, as measured by 10 ° of ion current versus temperature. Figure 11 shows the gas exhausted from the K2c〇3 / Rb2C〇3 / Cs2C〇3 catalyst. 10g0 ("log" ,,) of ion current plotted against temperature ("τ").

㈣168 # 17G is the value of h 1G of the water discharged from the inorganic salt catalyst and its ion current. The turning point from this inorganic salt catalyst 触 appeared at 360. 〇 3 catalysts in contrast, both potassium carbonate and carbonic acid have undetectable electricity and K2C03 / Rb2C03 / Cs2C0 at 3 60 ° C for the discharged water and the secondary turning point. The inorganic salt formed by the catalyst's actual organic salt in the exhaust gas is confirmed by the increase in mass of K2C03 / Rb2C03 / Cs2C03. Two or more different media can be more disordered than individual pure carbonates. 93 200533738 Example 6. DSC test of inorganic salt catalysts and individual inorganic salts. In all DSC tests, 10 mg samples were heated at a rate of 10 cc per minute to 520 ° C, at a rate of 10 per minute. Rates from 520. (: Cooled to 0 ° C, and then heated from 0 to 10.0 ° C per minute using a differential scanning calorimeter (DSC) DSC-7 type (manufactured by Perkin-Elmer (Norwalk, Connecticut, USA)) 600. (: K2C03 / Rb2C03 / Cs2C03 catalyst DSC analysis during the second heating of the sample showed that the salt mixture exhibited a wide thermal transition between 2 1 9 C and 2 6 0 C. The The midpoint of the temperature range is 25 °. The area under the thermal transfer curve is calculated as _1_75 Joules / gram. The start of crystal disorder is determined to start at the minimum DSC temperature of 219. Contrary to these results, for No clear thermal transition was observed with carbonated planers. DSC analysis of Li2C03, Na2C03, and K2C03 mixtures during the first-person heating cycle showed that Li2C03 / Na2CCVK2C03 mixtures exhibited temperatures between 390 C and 400 ° C. A sharp thermal transition. The midpoint of this temperature range is 385. (:. The area under the thermal transition curve is calculated as -182 Joules / gram. The onset of migration is determined to be a minimum of 39.0. DSC temperature begins. Sharp thermal transitions indicate essentially homogeneous salts All the test systems for the red level of n and organic salts relative to n were performed as follows: · Place the 81 81 cm (H inch) inorganic salt catalyst or individual inorganic salts in a muffle furnace (fm, nace)-one There are uranium wires separated from each other but immersed in the sample. The quartz wires are connected to these. These metal wires are connected to a 9.55 volt dry electricity 94 200533738 cell and a 220,000 ohm current-limiting resistor. The furnace was heated to 600 ° C and the current was measured using a microampere meter. Figure 12 shows the sample resistance versus carbonic acid removal resistance ("10 g (rk〗 c0),) vs. temperature (" T ") The graph of the log plot. The curves 172, ι74, n6, 178 and 180 are K2C03 resistance, CaO resistance, K2C03 / Rb2C03 / Cs2C03 catalyst resistance,

I2g of Li2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst resistance and Na2C03 / IC2C03 / Rb2C03 / Cs2C03 catalyst resistance.

CaO (curve 174) exhibits a considerable stable resistance relative to K2CO3 (curve 1 72) at a temperature in the range of 38-500 ° C. Stable resistance indicates an unordered structure and / or does not tend to separate and move ions from one another during heating. K2C〇3 / Rb2C〇3 / Cs2C〇3 catalyst,

Ll2C03 / K2C03 / Rb2C〇3 / Cs2C〇3 ^ ^ Na2C03 / K2C03 / w ^ 〇3 / cS2C〇3 catalysts (see curves 176, 178, and 18〇) are within the range of 35. Shows a sharp decrease in resistivity relative to K2CO3 at temperature. A decrease in resistivity is usually expressed when a voltage is applied to an inorganic salt embedded in it.

:: A: A current was detected during the metal wire. The data in Figure 12 confirm that inorganic salt catalysts are generally more mobile than pure surplus salt at temperatures in the 0 C range. Persistence ^ 13 is Na2C〇3 / K2C〇3 / Rb2C〇3 / CS2C〇3 catalyst resistance relative graph / C03 resistance ("1〇g (Γ Κ ^ 〇3),) vs. temperature (" T ”) The diagram of the log graph. Qu _ i π Na2C〇3 / K2C〇3 / Rb2C〇3 / Cs2C〇3 For κ Β, the Na2C〇3 / K2c〇3 / Rb2co3 / cs2co3 catalyst resistance phase '2C03 resistance (curve 172) is plotted against temperature. After adding 95 200533738 heat, the Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst is cooled to room temperature and then heated in a conductive device. Curve 1 84 is after cooling from 600 to 25. (: After that, during the Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst heating, the inorganic salt catalyst resistance is plotted against the K2C03 resistance versus temperature Iog. Reheated Na2C03 / K2C03 / The ionic conductivity of the Rb2C03 / Cs2C03 catalyst is increased compared to the original ionic conductivity of the Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst. «Δ myoelectric salt catalyst ion conductivity during the first and second heating It can be inferred that the inorganic salt catalyst forms a different form (the second form) when it is cooled, and it is different from the form before any heating (the Form) Different. Complex 8. Fluidity test of inorganic salt contact: A powdery K / CVRhCCVChCO3 catalyst with a thickness of 2 cm was placed in a quartz plate. The plate was placed in a furnace and heated to 500 ° C. 0C lasted i hours. To measure the flow properties of the catalyst, the tray was manually tilted in an oven after heating. 2C03 /; Rb2C03 / CS2C03 catalyst did not flow. When pressed, the remote catalyst has the consistency of toffee. In contrast, individual carbonates are free-flowing powders under the same conditions. Only under the same conditions, the Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst becomes The liquid is easy to flow (for example, similar to water). ', • The crude oil feed is in contact with the oxygen source at A? • The following procedures and general procedures are used in Examples 9-27, except where the variables are described. 96 200533738: $ L HastelloyCP Gravity Heater (ParrModel, rated at 35 MPa operating pressure (50000_) at 500 ° C), it is equipped with an organic mixer and is located to enable the autoclave to be kept in the surrounding area for additional production E⑽ to 625% 5 〇C—Watt on the controller ^: Belt heating , Gas inlet, steam inlet, an outlet and an internal thermocouple to record temperature δ hexyl Before heating, the autoclave over a glass cloth-based isolation. Adding container: Adding container (250ml, 316 stainless steel Hawk (h-) container) is equipped with controlled heating system, appropriate gas control room, pressure relief device, thermocouple, pressure gauge and high temperature control valve (Swag—let Valve # SS-4UW), capable of adjusting hot, viscous and / or compressed crude oil feeds at a flow rate of 0-500 g / min. After filling the crude oil feed into this addition vessel, an outlet side of the high temperature control valve was connected to the first inlet of the reactor. Prior to use, the add container line is isolated. Product collection. The vapor from the reactor exited from the reactor outlet and was sent to a series of decreasing temperature cold traps (immersion tubes connected to a series of 150 ml, 316 stainless steel Hawker vessels). The liquid from this vapor is broken up in the cold trap to form a gas stream and a liquid condensate stream. If necessary, adjust the flow rate of vapor from the reactor and through the cold trap using a waste adjustment valve. The flow rate and total gas volume of the gas leaving the cold trap are measured using a wet test meter (Ritter Model # TG 05 Wet Test Meter). After leaving the wet flowmeter, the airflow is collected in an air bag (a Tedlai gas sampling bag) for analysis. GC / MS (Hewlett-Packard Model 5890, now Agilent Model 5890; Agilent Technologies, Zion 97 200533738

Illinois, manufactured by U.S.A.). The liquid condensate stream is removed from the cold trap and weighed. The crude product and water are separated from the liquid condensate stream. The crude product is weighed and analyzed. Procedure · Fill Cerro Negro (137.5 g) into the addition container. The crude feed has an API specific gravity of 6.7. The crude oil feed had a sulfur content of 0.042 grams, a nitrogen content of 0.011 grams, and a total Ni / V content of 0.09 grams per gram of crude oil feed. The crude feed was heated to 150 ° C. K2C03 / Rb2C03 / Cs2C03 catalyst (31.39 g) was charged into the reactor. The K2C03 / Rb2C03 / Cs2C03 catalyst system was prepared as follows: 16.44 g of K2C03, 19.44 g of Rb2C03 and 24.49 g of Cs2C03 were combined. The K2C03 / Rb2C03 / Cs2C03 catalyst has a minimum TAP temperature of 360 ° C. The K2C03 / Rb2C03 / Cs2C03 catalyst has a DSC temperature of 250 ° C. Individual salts (K2C03, Rb2C03, and Cs2C03) did not exhibit DSC temperatures in the range of 50-500 ° C. The TAP temperature is higher than the DSC temperature of the inorganic salt catalyst and lower than the dsc temperature of individual metal carbonates. The catalyst was rapidly heated to 450 ° C at a normal pressure flow of 250 cm V of methane. After the desired reaction temperature was reached, steam was metered into the reactor at a rate of 0.4 milliliters per minute and methane at a rate of 25.0 cmv minutes. The steam and methane were continuously metered during the 2.6 hours while the crude feed was being fed to the reactor. The crude oil feed was pressurized into the reactor with 16H for 5 minutes using 丨 5 Mpa (229 psi) cH4. After the addition of the crude feed was completed, the remaining crude feed (0.56 g) remained in the addition vessel. A decrease in temperature to 370 was observed during this crude feed addition. The catalyst / crude oil feed mixture was heated to a reaction temperature of 45 ° and held at 4 ° C for 2 hours. After two hours, the reactor was cooled and the resulting residue / catalyst mixture was weighed to determine the percentage of coke produced and / or not consumed in the reaction. The difference between the weight of the starting catalyst and the weight of the coke / catalyst mixture shows that 0.046 grams of coke per gram of crude oil feed remained in the reactor. The complete product contains 0.87 grams of crude oil product and gas with an average APr specific gravity of 13. The gas contains unreacted Cl, hydrogen, daggers and hydrocarbons, and CO2 (0.08 g of CO2 per gram of gas). This crude oil product contains 0.01 grams of sulfur and _ 0.000005 grams of culprit and V per gram of crude oil product. The crude product was not analyzed further. In Example 10, the reaction steps, conditions, crude oil feed and catalyst were the same as in Example 9. The crude product of Example 10 was analyzed to determine the boiling range distribution of the crude product. The crude oil product contained 0.14 grams of light oil, 019 grams of distillate, 0.45 grams of VG0 and 0.001 grams of residue per gram of crude oil product, and undetectable amounts of coke. Examples 9 and 10 demonstrate the contact of a crude oil feed with a hydrogen source in the presence of up to 3 grams of catalyst per 100 grams of crude feed to produce a complete product comprising a crude product that is a liquid mixture at STp. The crude oil product has a residue content of at most 30% of the residue content of the crude oil feed. The crude product has a sulfur content and a total Ni / V content of up to 90% of the sulfur and Ni / V content of the crude feed. The crude oil product contains at least 0.001 g of hydrocarbons having a boiling range of up to 200 at 0.001 Mpa, and at least 0.001 g of a boiling range of 200.300 at 0.001 MPa. (: Hydrocarbons between, at least 0.001 g 99 200533738 hydrocarbons with a boiling range between 400_538 (100F) at 0.101 MPa. __ · The existence of TL in the raw material and hydrogen source in the steam Contact · The reaction steps and conditions in Examples 11 and 12 and the KfCVRhCCVChCO3 catalyst system were the same as in Example 9, but using 130 g of crude oil feed (CerrONegr0) and 60 g of K2CC ^ Rb2C03 / CS2C03 Catalyst. In Example i !, methane was used as the hydrogen source. In Example 12, hydrogen was used as the hydrogen source. The diagram of the non-condensable gas, crude oil products, and coke content is depicted in Figure 14. Bar 186 And 188 _ represent the weight% of coke produced, strips 190 and 192 represent the weight% of produced liquid hydrocarbons, and Changmen 94 # 口 196 represents the weight% of produced gas. In Example 11, 93% by weight of crude oil product (strip 192), 3% replacement gas (strip 196) and 4% by weight coke (strip 188) were prepared. Based on the weight of Cerro Negro. In Example 12, 84% by weight of crude oil product (long bar 19〇), 7% by weight of gas (long strip 194) and 9% by weight of coke (long strip 186), φ This is the weight of Cerro Negro. 施 Only examples 11 and 12 provide the use of a courtyard as a hydrogen source Compared with the use of hydrogen as a hydrogen source. Kraft is generally cheaper to manufacture and / or transport than hydrogen, so the method of using Kraft is ideal. As proven, 'the crude oil feed is contacted in the presence of an inorganic salt catalyst When manufacturing a complete product, methylbenzene is at least as effective as hydrogen source as hydrogen. Specific gravity of crude oil product · 100 200533738 Equipment, reaction steps and inorganic salt catalyst system are the same as those described in Example 9, but the reactor pressure is changed Example 13 'The reactor pressure during the contact was 0.1 MPa (14.7 psi). A crude oil product with an API specific gravity of 25 was obtained. The complete product had hydrocarbons with a carbon number distribution in the range of 5 to (See curve 198 in Figure i $). In Example 14, the reactor pressure during the contact was 3.4 Mpa (514.7 ps.). A crude oil product having an Aρ specific gravity of 516 at 15 5c was produced.

Thing. The complete product has hydrocarbons with carbon numbers ranging from 5 to 15 (see curve 200 in Figure 15). Some examples of a crude oil feed are contacted with hydrogen in the presence of an inorganic salt catalyst at different pressures to produce a crude oil product having a selected API specific gravity. Or lower Aρι specific gravity crude products. Contact of Emperor Enonu · Zaihui

In _16, the clothes setting, crude oil feeding and reaction steps are the same, but the crude oil feeding and contacting f 1 q W medium (or &amp; cutting) are directly loaded into the reactor at the same time. Such as — 2 ″ 1 at first is milk. Cerro Negro virtual 60 4 in the implementation of Example 1 5 5 5 4 5 5 5 5 5 2 K2C03 / Rb2C03 / Cs2C〇3 Rabbit (the same catalyst as in the case of palladium 9) . In Example 16, 13 grams of Cerro Negro and 83.13-year-old Ishido Park Α /

Materi.l · Λ1 gram of anaerobic silicon (40 mesh, Stanfor ls, Alls Viejo, CA) | | This silicon carbide is believed to have (if any) low catalyst properties under the method conditions described in 4. 101 200533738 In each sample 'the mixture was heated to 500 during 2 hours. . The response suitability. will. 〇2 Measured to the reaction at a rate of 100 cm 3 / min. Using 3.2 MPa (479 7 Osi) &amp; η wide V 479.7 PS1) will be collected from the reactor in the cold trap and air bag. Will come from, into ... milk analysis. The sanitary knife was prepared in Example 15 from the contact between the crude oil feed and the inorganic salt catalyst under a carbon dioxide atmosphere of 36. (2 "8% by weight, based on the weight of the crude oil material) API A colorless hydrocarbon liquid with a specific gravity of at least 50. In Example 16, 15.78 g (11.95 wt%, based on the weight of tritium) of API was 12 from the contact of the crude oil feed with the carbonized rock under a carbon dioxide atmosphere. The API specific gravity was 12 Yellow hydrocarbon liquid.

Although the yield in Example 15 is very low, the on-site generation of hydrogen source in the presence of an inorganic salt catalyst is greater than the on-site generation of hydrogen in the absence of a catalyst. The yield of the crude product in Example 16 was half the yield of the crude product in Example 15. Example 15 also confirmed that tritium was produced during the contact of the crude oil feed in the presence of inorganic salts and the absence of a gaseous hydrogen source.

Examples 17-20 ·· Crude oil and oil materials ^ 2CQ_a_Li—Medium, calcium oxide and silicon carbide are stored under your normal pressure bar #, installation steps, crude oil feed and inorganic salt catalyst system The same as in Example 9 'but adding Ceiro Negro directly to the reactor instead of adding via an addition vessel' and using hydrogen as a hydrogen source. The reactor pressure during the contact was 0 · 101 MPa (14.7 psi). The hydrogen flow rate was 250 cm 3 / min. The series of reaction temperatures, steam flow rates, and percentages of crude product, gas, and coke produced are shown in Table 4 in Figure 16. 102 200533738 In Examples 17 and 18, K2C03 / Rb2C03 / Cs2C03 catalysts were used. In Example 17, the contact temperature was 375. In Example 18, the contact temperature was within a temperature range of 500-600 ° C. As shown in Table 4 (Fig. 16), for Examples 7 and 8 when the temperature is from 375. (: Increasing to 500 cC, gas production increased from 0.02 g per gram of complete product to 0.05 g of gas. However, coke production decreased at higher temperatures from 0.17 g per gram of crude feed to 0.00 9 grams of coke. The sulfur content of crude oil products has also been reduced from 0.01 grams per gram of crude oil products to 0.008 grams of sulfur at higher temperatures. The two crude oil products are all workable. The crude oil feed was contacted with CaCO3 under conditions similar to those described in Example 18. The series of percentages of crude oil products, gas, and coke production are shown in Table 4 in Figure 16. The gas production is in the opposite of Example 19, The gas production in Bayesian Example 18 is increased. The effect of removing crude stone from the feed of crude oil is not as effective as that in Example 8. Compared to per gram of crude oil product produced in Example i 8 The sulfur content of the crude oil product was 0.88 grams, and the crude oil product produced in Beige Example 19 contained 0 grams of sulfur per gram of crude oil product. Example 20 is a comparative example of Example 18 in the implementation. In Example 20, 83.13 g of silicon carbide was charged into the reaction instead of the inorganic salt catalyst. The production of gas and coke in Beizhi Example 20 is increased compared to the production of S and coke in Example 1 $. Under these catalyst-free conditions, the per gram of crude oil produced is 4 0.22 Grams of coke, 0.25 grams of non-condensable gas, and 0.5 grams of crude oil products. Compared to 0.001 grams of sulfur 'per gram of crude oil products produced in Example 18 The crude oil product is 103.33 gram per gram of crude oil product. The oil product contains 0.036 g of sulfur. 14 Some examples demonstrate that the catalysts used in Examples 17 and 18 provide superior catalyst conditions and conventional metal salts. Improved results. At a hydrogen flow rate of 5000c and 25cm cm, the amount of coke and non-condensable gas is significantly lower than the amount of coke and non-condensable gas produced under catalyst-free conditions. In the example of the salt catalyst (see the practical examples 1 7-1 8 in Table 4 of FIG. 16), compared to the gas formed during the control experiment (for example, Example 20 in Table 4 of FIG. 16), The reduction in the weight percentage of the produced gas was observed. From the amount of hydrocarbons in the produced gas, the Luther of the crude oil feed was estimated Cracking is up to 20% by weight, up to 15% by weight, up to 10% by weight ^ to $ 100% by weight or none, based on the total amount of crude oil feed in contact with the hydrogen source. ~ * Exempt Examples ~ and 22-:- A ... Oil feed—feed and gaseous radon sources are stored in the presence of water-disrupted or disrupted media. The devices in Examples 21 and 22 are the same as in Example 9, but hydrogen is used as the hydrogen source. In Example 21, 10.4 g of Cerr〇 心 ^ 〇 and 3088 g of ICCVRlCCVC ^ CO3 catalyst were combined to form a crude oil feed mixture. In yoke example 22, 139.6 Grams of Cerro Negro were combined with 80.14 grams of rock-anhydrite fossil to form a crude oil feed mixture. The crude oil feed mixture was charged directly into the reactor. Hydrogen was metered into the reactor at 250 cmV during heating and residence. The crude feed mixture was heated to 300 over a period of 15 hours. And maintained at 3⑻. c down ^ hours. The reaction temperature was increased to 400 during 1 hour. . And maintained at 400 ° C for 1 hour. After the reaction temperature reached 400, water was fed into the reactor at a rate of g / 104 200533738 minutes to combine with hydrogen. Water and hydrogen were metered into the reactor to maintain heating and residence time. After maintaining the reaction mixture at 400 ° C., the reaction temperature was increased to 500 ° C .: and maintained at. 2 hours below. The vapor generated by the reactor was collected in a cold trap and an air bag. The liquid product from the cold trap was consolidated and analyzed. In yoke example 21 '86.17 g (66.1% by weight based on the weight of the crude feed) dark reddish brown hydrocarbon liquid (crude product) and water (97 · 5 g ) It is generated from the contact between crude oil feed and K m AX IT ”iv2LU3 / Rb2C03 / Cs2C03 catalyst under hydrogen atmosphere. In Example 22, water vapor and a small amount of gas are generated from the reactor. Check the reactor and remove the dark brown viscous hydrocarbon liquid from the reactor. The contact of the crude feed with silicon carbide under a hydrogen atmosphere produces less than 50% by weight of a dark brown viscous hydrocarbon liquid. Compared to Example 22 Yield of the crude oil product produced. A 25% increase in crude oil product yield was observed in Example 21. Example 21 demonstrates that the properties of the crude oil product produced using the method described herein are improved relative to the crude oil product produced using hot water. . Specifically, in the implementation The crude oil product in Example 21 has a lower boiling point than the crude oil product obtained from Example 22, as the crude oil product produced in Example 22 cannot be proven to produce steam. Compared to the crude oil product produced in Example 22 The crude oil product produced in Example 21 has enhanced flow properties, as determined by visual inspection. · · Contact under the crude oil feed, crude oil with a 1 liter volume increased by immersion in crude oil produced by IE. Substrate setting, 105 200533738 Crude oil feed, inorganic catalyst and reaction steps are the same as those described in Example 9 ', but the crude oil feed is directly charged to the reverse storage, the clothes are set to the response state and hydrogen is used as Gas source. The crude oil feed (cerroNegro) has a specific gravity of 6. 7 and a density of 1.02 g / ml at i55 ° C. In Example 23, 102 g of crude oil was fed (100 ml of crude oil). Feed) and Mg of l ^ / Rb ^ O ^ hCO3 catalyst were charged into the reactor. A crude oil product of 079696 g / ml (112 ml) at an API specific gravity of 50 and a density of 1550c was prepared. 87 6 grams). In Example 24, 102 grams of crude oil was fed (100 milligrams). Raw # oil feed) and 80 g of silicon carbide were charged into the reactor. A crude product (70 g) of 0.9861 g / ml (70 ml) at an A2 specific gravity of I2 and a density of 15.5 V was produced. Under these conditions Next, the volume of the crude oil product obtained from Example 23 is approximately 10% greater than the volume of the crude oil feed. The volume of the crude oil product produced in Example 24 is significantly less than (40% less) than the crude oil produced in Example 23. Product Volume. A significant increase in product volume increases the ability of a manufacturer to produce more volume of crude oil product per volume of crude oil input. · 1_ Example 2 U oil feed and hydrogen source at K, CO, /RKr〇./rLr〇i — — — — — — Contact of the media, sulfur and AAA under the device and reaction steps are the same as in Example 9 The above is the same, but the steam is metered into the reactor at 300 cm &quot;. The K2C03 / Rb2C03 / Cs2C03 catalyst is prepared by combining 27.2 grams of K2C03, 32.2 grams of Rb2C03, and 40.6 grams of Cs2C03. Crude oil feed (130.35 g) and K2C03 / Rb2C03 / Cs2C03 catalyst (3 1.6 g) were charged into the reactor. Cerro Negro Crude Oil per gram of original 2005 200533738 oil feed contains 0.04 grams of total aromatics with a boiling range distributed between M9_26 ° c (300 ° _5 ° F), 0.0064 g of combined Nickel and vanadium, 0.042 g of sulfur A, 0.56 g of residue. The crude gravity of the crude feed was 6.7. The contact of the crude feed with methane in the presence of the K / CVRb / CVCsfh catalyst was' per gram of crude feed, which produced G.95 grams of the complete product and 0.041 grams of Coke. The complete product contains 091 grams of crude product and 0.028 grams of hydrocarbon gas per gram of complete product. The total gas system collected contains π mole of hydrogen, 0.045 mole of carbon dioxide, and 025 moles of dagger and C6 smoke, as determined by GC / MS. The remainder of the gas is methane, air, carbon dioxide, and traces (0 · _mol) of evaporated crude oil products. The crude product was analyzed using a combination of gas chromatography and mass spectrometry. The crude product contains a hydrocarbon mixture with a boiling range between 538% fresh. The total liquid product mixture was composed of 006 g of ethylbenzene per gram of the mixture (a monocyclic cyclic compound having a Buddha point of 136.2 OC at 0.101 MPa). This product was not detected in the crude feed. The used catalyst ("first used catalyst") was removed from the reactor,% weight, and then analyzed. The weight of the first used catalyst was increased from 3 to 6 grams to a total weight of 37 to 38 grams (based on the original K2C03 / Rb2C03 / Cs2C ... catalyst weight, an increase of 8% by weight). The first used catalyst system contained 0.15 g of extra coke, 〇35 g of sulfur, 0.001 g of Ni / V, and 0.845 g of K2C03 / Rb2C03 per gram of used catalyst. / Cs2C〇3. The extra-jaw crude oil feed (152_71 g) was contacted with the first used catalyst 107 200533738 (36.63 g) to make a gram of recovered complete product after loss. The complete product was 0.92 grams of liquid crude product '0.058 grams of additional coke and 0.017 grams of gas per gram of complete product. The gas system contains 0.18 moles of hydrogen, 0.07 grams of carbon dioxide, and 0.35 moles of C ^ C: 6 hydrocarbons per mole of gas. The remainder of the gas is methane, nitrogen, some air, and traces of evaporated petroleum products (&lt; 丨% mole). The crude product contains a hydrocarbon mixture with a boiling range of 100-538. Part of the mixture whose boiling range is below 149 ° C is based on 0.018 mole% ethylbenzene per mol of total liquid hydrocarbons, 0.004 mole% methylbenzene, 0.03 mole% methane Toluene and 0,060 mole% p-xylene (monocyclic cyclic compounds having a boiling point of 149 or less at 0.101 MPa). These products were undetectable in the crude feed. The used catalyst ("second used catalyst,") was removed from the reactor, weighed, and analyzed. The weight of the second used catalyst was increased from 36 to 63 grams to a total weight of 45.44 grams ( Based on the original K2C (VRb2C ... / Cs2C03 catalyst weight, an increase of 43% by weight). The second used catalyst system contains 0.32 g of coke per gram of the second used catalyst. 〇1 g of sulfur and 0.67 g. An additional crude oil feed (104 g) was contacted with the second used catalyst (44.84 g) to make 1 per gram of crude oil feed. 4 grams of complete product, and collected 0.114 grams of coke. Since 1 44.1 grams of crude oil feed was conveyed for 133 grams of crude oil, a part of the coke was attributed to the addition of the container due to excessive heating in the addition container The resulting coke. The complete product is 0.88 grams of crude product and 108 200533738 0.025 grams of hydrocarbon gas per gram of complete product. The total gas system contains 0.18 moles of hydrogen and 0.052 moles per mole of gas. Carbon dioxide and 0.03 moles of C2-C6 hydrocarbons. The remainder of the gas is oxane, air, carbon monoxide, Hydrogen sulfide and a small amount of evaporated petroleum. The crude oil product contains a hydrocarbon mixture with a boiling range of 100-538 0C. The mixture with a boiling range of less than 149 ° C is partly composed of 〇_〇21 grams Ethylbenzene, 0.027 g of toluene, 0.042

G of m-xylene and 0.020 g of para-xylene, as previously determined by GC / MS. The used catalyst ("third used catalyst,") was removed from the reactor, weighed, and analyzed. The weight of the third used catalyst was increased from 44.84 grams to a total weight of 56.59 grams (Based on the original K2co3 / Rb2C03 / Cs2C03 catalyst weight, an increase of 79% by weight.) Detailed elemental analysis of the third used catalyst. The third used catalyst is an additional substance per gram Contains 0.90 grams of carbon, 0.028 grams of hydrogen, 0.025 grams of oxygen, 0.0046 grams of sulfur, 0.007 grams of nitrogen, 0.0018 grams of vanadium, and 0.0007 grams of nickel , 〇〇〇15

Grams of iron and 0.0025 grams of gas ions, and the rest are other transition metals, such as chromium, titanium, and hafnium. As confirmed in the example, the deposition on the inorganic salt catalyst and: two =: and / or metal does not affect the crude oil product produced by the contact with the hydrogen through the crude oil feed ... the organic salt catalyst The total yield is inconsistent. The crude product was boiled below 14 "c. The original material was contained in the cloth, and the content of the monocyclic aromatic compound was 100 times that of the monocyclic cycloaromatic 4 compound. 109 200533738 For these three tests, the average The crude product yield (based on the weight of the crude feed) was 89.7% by weight 'standard deviation was 26%; the average charcoal yield was 7.5% by weight (based on the weight of the crude feed) with a standard deviation of 2.7 % 'And the average weight yield of gaseous cracked hydrocarbons is 23% by weight (based on the weight of crude oil feed)' standard deviation is 0. The larger standard deviation of both liquid and coke is due to the third test The temperature controller of the feeding container was caused by a malfunction, and the crude oil feed in the adding container was overheated. Even so, even the large amount of coke tested here did not have a significant and significant adverse effect on the activity of the catalyst system. The ratio of total C2 is 0.19. The ratio of C: 3 olefins to total c3 is 0.4. The ratio of a fine smoke of C4 smoke to the dilute hydrocarbons in the molecule is OH. The cis / transene smoke ratio is 6.34. This The ratio is considerably higher than the predicted 0.868 thermal activity C4 cis / trans olefin ratio. The ratio of α5 olefins to intramolecular olefins of C5 hydrocarbons is 0.92. This ratio is larger than the predicted thermodynamic c5 α-hydrocarbons to I intramolecular olefin ratio. Ishun / The anti-olefin ratio is 1.25. This ratio is larger than the predicted thermodynamic c5 cis / anti-olefin ratio of 0.9. Example 26: Contact · device in the presence of a right-catalyzed crude oil feed tray with a relatively high sulfur content The reaction steps are the same as those described in Example 9 except that the crude oil feed, methylbenzene, and steam are continuously fed into the reactor. The content of the feed in the reactor is monitored by using the change in the weight of the reactor. The methane gas was continuously metered into the reactor at 500 cm 3 / min. The steam was continuously metered into the reactor at 6 g / min. The inorganic salt catalyst was passed through 27.2 g of κβ〇3, 32 2 g of Rb2C03 and 40.6 grams of Cs2C03 is obtained by combining the K2C03 / 110 200533738

Rb2C03; _CS2C03 catalyst (59.88 g) was charged into the reactor. Eight. A crude oil feed (asphalt, Rammings, Canada) with an API specific gravity of 9.4, a sulphur content of 0.02 grams of sulfur and a residue content of 0.40 grams per gram of crude oil feed was heated to 15 in an addition vessel. 〇c. The heat transfer was continuously metered into the reactor at 1 0.5 g / min from Tiangu in an attempt to maintain the crude oil feed level at 50% of the reactor volume; however, the rate was not sufficient to maintain the level. The methane / steam / crude oil feed was in contact with the catalyst at an average internal reaction of 4% per dish. The contact of the methane / steam / crude oil feed with the catalyst produces a complete product (in this example, it is in the form of steam flowing out of the reactor). A total of 1640 grams of crude feed was processed over a 6 hour period. From the difference between the weight of the starting catalyst and the weight of the crumb / catalyst mixture, it is known that from 0 to 85 g of coke per gram of crude oil feed remained in the reactor. From the contact of crude oil feed with methane in the presence of K2C ^ 3 / Rb2C03 / Cs2C03 catalyst, 0.93 g of complete product was obtained per g of crude oil feed. This complete product is a product containing 0.03 grams of gas and 0.97 grams of crude oil per gram of complete product, excluding the amount of methane and water used in the reaction φ. The gas system contains 0.014 grams of hydrogen per gram of gas, 0.018 grams of carbon monoxide, 0.13 grams of nitrogen sulfide, and non-condensable hydrocarbons. From the amount of hydrogen sulfide produced ', it is estimated that the sulfur content of the crude feed was reduced by 18% by volume. As shown in this example, tritium hydrogen, carbon monoxide, and carbon dioxide are generated. The molar ratio of carbon monoxide to carbon dioxide is 0.4. The CVC5 tobacco series contains 0.30 grams of dagger compounds, 0.332 grams of C: 3 compounds, 0.26 grams of C4 compounds, and 0.10 grams of C5 compounds per gram of smoke. The weight ratio of isopentane to n-pentane in the non-condensable fes was 0.3. The weight ratio of isobutane to n-butane in non-condensable hydrocarbons was 0.189. The c4 compound has a butadiene content of 0.0003 g per gram of the C4 compound. The weight ratio of aC4 olefin to intramolecular C4 olefin was 0.75. The weight ratio of aq olefin to c5 olefin in the molecule was 1.08. The data in Example 25 confirmed that the continuous processing of a relatively high sulfur crude feed and the same catalyst in the presence of coke did not impair the activity of the inorganic salt catalyst and produce a crude product suitable for transportation. Example 27: The two crude oil feeds and the nine gens at / Cs, the CO3 catalyst, and the carbon deposition and reaction steps were performed using the conditions described in Example 26. The K2C (VRb2C (VCs2c03 catalyst (56.5 g) was charged into the reactor. A total of 2550 g of crude oil feed was processed during 6 hours. From the difference between the initial catalyst weight and the weight of the residue / catalyst mixture It can be known that based on the weight of the crude oil feed, 0.4 g of coke per gram of crude oil feed is left in the reactor. Each gram of crude oil feed produces a total of 0.89 grams of complete product. The complete product is per gram The complete product contains 0.004 grams of gas φ and 0.96 grams of crude oil product. The amount of methane and water used in the reaction does not include the amount of methane and water used in the reaction. The gas system contains G. 21 grams of hydrogen per gram of gas, 8 grams -Carbon oxide, 0.052 grams of carbon dioxide, 0.18 grams of hydrogen sulfide, and 0.65 grams of non-condensable hydrocarbons. From the amount of hydrogen sulfide produced, it can be estimated that the sulfur content of the crude oil feed has been reduced. It is based on the weight of crude oil feed. As shown in this example, there are hydrogen, -oxidation and carbon dioxide generation. Monooxygen 112 200533738 Molar ratio of carbonized carbon dioxide to carbon dioxide is 0.6. C2-C6 hydrocarbons It contains 0.44 grams of C2 compounds and 0.31 grams of C3 compounds per gram of C2-C6 hydrocarbons. 0.19 grams of C4 compounds and 0.068 grams of C5 compounds. The weight ratio of isopentane to n-pentane in non-condensable hydrocarbons is 0.25. The weight ratio of isobutane to n-butane in non-condensable hydrocarbons is 0 · 15. C4 compounds have a butadiene content of 0.003 grams per gram of C4 compound.

This example demonstrates that the repeated processing of a relatively high sulfur crude oil feed (2550 g of crude oil feed) and the same catalyst (56.5 g) in the presence of coke has not impaired the activity of the inorganic salt catalyst, and a crude oil suitable for transportation has been prepared product.

In view of this description, modifications and alternative specific examples of various aspects of the present invention will be apparent to those having ordinary knowledge in the technical field to which the present invention pertains. Therefore, this description should be construed as an example only and for the purpose of teaching the ordinary people skilled in the art to which the present invention pertains to implement the present invention. It should be understood that the forms of the invention shown and described herein are examples to be taken as specific examples. Elements and materials can replace those exemplified and described herein, the number of copies and procedures can be reversed, and certain features of the present invention can be independently used. After benefiting from the description of the present invention, all will be the technical field to which the present invention belongs It is understood by those with ordinary knowledge. Changes may be made in the elements described herein without departing from the spirit and scope of the invention as set forth in the following patent claims. x [Brief description of the drawings] The attached drawings will more clearly illustrate the advantages of the present invention. With the help of the above detailed description and reference, a person with ordinary knowledge of the technical field to which the present invention pertains, the figure: 113 200533738 A schematic illustration of a specific example of a contact system for contacting a crude oil feed with a hydrogen source in the presence of one or more catalysts to produce a complete product. Fig. 2 is a diagram showing another specific example of a contact system for contacting a crude oil feed with a hydrogen source in the presence of one or more catalysts to produce a complete product. Figure 3 is a specific example of a separation zone combined with a contact system. Figure 0 is a specific example of a blended zone combined with a contact system.

Fig. 5 is a diagram showing a specific example of a separation zone, a contact zone and a blending zone. ~ Figure 6 is a schematic diagram of a specific example of a multiple contact system. FIG. 7 is a schematic diagram of a specific example of an ion conductivity measurement system. Figure 8 is a list of crude oil feed properties and crude product properties obtained from conventional examples of contacting a crude oil feed with a transition metal sulfide catalyst. Figure 9 is a tool for contacting a crude oil feed through a dagger and a catalyst

"The list of crude oil feed composition and non-condensable hydrocarbon composition obtained in the example. The figure is a list of properties and composition of crude oil products that have been dispensed with by contacting the crude oil feed with the transition metal sulfide catalyst. Fig. 11 is the ionic inorganic salt catalyst exhaust gas 7JT, which is plotted against the log 10 of the temperature as measured by TAP. Fig. 12 is the inorganic salt catalyst and inorganic relative to the potassium carbonate resistance. A graph of the log 1 of the salt I and the ratio of ions / degree. Figure 13 is the Na2C〇3 / K2C〇3 / Rbc 114 200533738 catalyst resistance vs. γ β 7 versus the ratio of potassium carbonate resistance. h] 〇 Illustrated diagram. Material imaginary = 4 is a diagram of who is the coke, liquid smoke and gas for various different oils. For the specific example of the weight percentage of hydrogen source, H 15 is from A graph showing the percentage of carbon versus carbon number for the crude oil feed in contact with the inorganic salt catalyst and the fragrant π γ ~ green produced by the crude oil product. Figure 1 6 And ... a list of ingredients made from specific examples of osmium salt catalysts, metal salts or silicon carbide contact. It is easy to have specific examples for the A 杳 彳 μ ② generation form, but it is shown in the diagram with its special and J first examples. It is clear that the scheme can be a L and will be explained in detail in this article. The month b is not drawn to scale. It should be understood that ... the description is not intended to limit the invention to the disclosed particular schema and its details. The invention is intended to cover the spirit and scope of the invention: 9 All changes and descriptions of [Key component symbols] 100 Contact system 101 Crude oil supply source 102 Contact area 104 Conduit 106 Conduit 108 Conduit 110 Flow control valve 110 'Flow control valve 112 Gas inlet 115 200533738 114 Steam Inlet 116 separation zone 118 conduit 119 crude product receiver 120 conduit 122 contact system 124 separation zone 126 conduit 128 conduit 130 contact system 132 separation zone 134 conduit 136 conduit 138 conduit 140 blending zone 142 conduit 144 conduit 146 multiple contact system 148 contact system 150 tube 152 tube 154 tube 156 quartz container 158 sample

116 200533738 160 162 164 166 168-170 172-180 182-184 186-188 190-192 194-196 198-200 Power metal wire metal wire meter ionic current vs. temperature plot resistance curve vs. temperature plot relative resistance curve Plotting temperature vs.% coke produced% wt. Liquid hydrocarbons wt% wt. Gas carbon distribution

117

Claims (1)

200533738 10. Scope of patent application: 1. A method for manufacturing a crude oil product, comprising contacting a crude oil feed with a hydrogen source in the presence of one or more catalysts to produce a crude oil product, wherein one or more of the catalysts include Catalyst containing K3Fe ^ Si4. 2. If the scope of patent application is the first! In this method, the ye-μ is formed on the spot. 3. The method according to item 1 or 2 of the patent application scope, wherein the one or more catalysts include at least one other transition metal sulfide. 4 _ A method of making a crude product, comprising: contacting a crude feed with a hydrogen source in the presence of one or more catalysts to produce a complete product comprising the crude product, wherein the crude product is at 25. . It is a liquid mixture with 0.101 Mpa. At least one of the catalysts contains one or more transition metal sulfides, and the crude oil feed has a residue content of at least 0.2 grams of residue per gram of crude oil feed, such as in ASTM method D53〇7. Measured; and controlling the contact conditions so that the crude oil product contains at most 0.05 g of coke per gram of crude oil product, wherein the weight ratio of atomic hydrogen to atomic carbon (H / C) in the crude oil product is at most h75 , As measured by ASTM method D6730. 5-A method of making a crude product, comprising: contacting a crude feed with a hydrogen source in the presence of one or more catalysts to produce a complete product comprising a crude product, wherein the crude product is at 25. Rhenium is a liquid mixture at 0.11 Mpa. At least one of the catalysts contains one or more kinds of transition metal sulfides, and the crude oil feed has a residue content of at least 0.2 grams of residue per gram of crude oil feed, such as ASTM As determined by method D5307, 118 200533738 and the atomic hydrogen pair in the crude oil feed are 1.5 and less; and the heavy weight ratio (H / C) of 7 is controlled to control the contact conditions, so that the crude oil product has 80-120% H / C ratio, the crude oil product has a residue content of 30% per gram / one mile, as determined by ASTM, 'the crude oil product contains at least' please 17 measured oil per gram of crude oil product ' And the light oil has a scorch value of at least 70. . Light 6. The H / C th ^ ^ ^ of item 5 of the patent application range, wherein the H / L ratio of the crude oil product is 90 · η0% of the H / C of the crude oil feed. Liao 7 · If any of the scope of the application for patents No. 4-6, the crude oil product residues, plutonium content up to ^,, method, of which δ Hai%. ... Li Zhixi is 10% of the residue content of the crude oil feed. If any of the scope of patent applications No. 3-7, at least one of the transition metal sulfides contains ... of which the transition metal, one or more options From the week to the Periodic Table of the &amp; metal compounds or mixtures thereof: dog 6.10 transition 9. If at least one of the scope of the patent application transition metal sulfide i0. As the scope of the patent application transition metal sulfide In the range of at least 10 · 5 -10. -The method of any of items S, wherein the transition metal is iron. The method of any item in item 3.9, wherein the atomic ratio of the transition metal to T, is the method of any item in item, wherein one or more alkali metals, the one or more alkaline earth metals, the one U. If the scope of the patent application is No. 3-10, the catalyst containing transition metal sulfides also contains one or more compounds of various alkali metals, 119 200533738 or one or more compounds of zinc, compounds, or their compounds. mixture. One or more of zinc 13. If any of the items in the patent application range 1.12_ are also controlled, the contact conditions are controlled such that during the contact, grams of crude oil per gram, at most 0.15 grams or at most 01 grams are formed with condensable hydrocarbons at 25 As determined by the mass balance 14. As in any of claims 1 to 13 of the scope of the patent application_ At least a part of the complete product is made by steam, including condensation at 25 ° C and 0.1 MPa at least one to form the crude product . Method, wherein the feed has at most 0.2 O.iOl MPa, and the method is not more than 0, and further, the method further comprises a part of the vapor to 1 5 · According to the scope of patent application 1-1 4 Crude oil products are grams of coke per gram of crude oil products. The method of any one of the items, 0.00001-0.03 grams or 〇. Among them 〇〇〇κ 16. As the method of any of the claims in the scope of claims -15, the method of recovering oil products is per gram of crude oil products. 〇〇1, · υ :) grams of residues &amp; 〇〇〇〇1-0.99 grams of vacuum gas oil, 〇〇〇〇〇.09, 0.001-0.2 grams of light oil or a mixture thereof. /night Crude residue. 17. The method feed according to any one of items 1 to 16 of the scope of the patent application. The feed of each method of crude oil feed contains 0.2-0.99 Shen Wu Λ Fan and 0.3. For example, the method of applying for any of the members in the patent scope No. ι_17, of which 120 200533738. The method further includes combining the crude oil product or different crude oils to form a same crude oil product. 9. Kinds of crude oil products Or a blend obtained by the method of any one of items 1-18. g is the second in the scope of Xinying's patent—a method of manufacturing fuel for ships and heating methods, which includes guards such as patents, intermediates, or chemicals or conjugates. 19th Crude Oil Product 21. The method of claim 20, wherein the processing includes distilling the crude product or the blend into one or more fractions. 2 2. If the method of applying for the patent scope is 20 or 21 items, the process may include hydroprocessing. Η ^ 一 、 Schematic: as the next page 121